EP1590076A1 - Reacteur tubulaire a enveloppe comprenant plusieurs zones pour l'execution de reactions exothermiques en phase gazeuse - Google Patents

Reacteur tubulaire a enveloppe comprenant plusieurs zones pour l'execution de reactions exothermiques en phase gazeuse

Info

Publication number
EP1590076A1
EP1590076A1 EP03701548A EP03701548A EP1590076A1 EP 1590076 A1 EP1590076 A1 EP 1590076A1 EP 03701548 A EP03701548 A EP 03701548A EP 03701548 A EP03701548 A EP 03701548A EP 1590076 A1 EP1590076 A1 EP 1590076A1
Authority
EP
European Patent Office
Prior art keywords
zone
tube reactor
jacket tube
reactor
reaction
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.)
Withdrawn
Application number
EP03701548A
Other languages
German (de)
English (en)
Inventor
Friedrich Gütlhuber
Manfred Lehr
Gunnar Heydrich
Gunther Windecker
Stephan Schlitter
Michael Hesse
Markus Rösch
Alexander Weck
Rolf Harthmut Fischer
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.)
MAN Energy Solutions SE
Original Assignee
MAN DWE GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by MAN DWE GmbH filed Critical MAN DWE GmbH
Publication of EP1590076A1 publication Critical patent/EP1590076A1/fr
Withdrawn legal-status Critical Current

Links

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
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/32—Packing elements in the form of grids or built-up elements for forming a unit or module inside the apparatus for mass or heat transfer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/26—Nozzle-type reactors, i.e. the distribution of the initial reactants within the reactor is effected by their introduction or injection through nozzles
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F28D7/0083—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium
    • F28D7/0091—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium the supplementary medium flowing in series through the units
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/22—Arrangements for directing heat-exchange media into successive compartments, e.g. arrangements of guide plates
    • 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
    • B01J2208/00212—Plates; Jackets; Cylinders
    • B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
    • 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
    • B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • 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
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/00849—Stationary elements outside the bed, e.g. baffles
    • 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
    • B01J2219/00245—Avoiding undesirable reactions or side-effects
    • B01J2219/00259—Preventing runaway of the chemical reaction

Definitions

  • Multi-zone jacket tube reactor for carrying out exothermic gas phase reactions
  • the invention relates to a multi-zone jacket tube reactor for carrying out exothermic gas phase reactions according to the preamble of claim 1.
  • the first zone in which the reaction proceeds most violently, is operated with circulation cooling by the same heat transfer medium as the evaporation zone following upwards, which is driven through a cooler by means of a circulation pump as it heats up in the reactor from the gas inlet.
  • a constant heat transfer medium temperature is inevitably set according to the heat transfer temperature of the first zone.
  • the steam generated in the evaporation zone is separated in a separator (steam drum) from the undevaporated heat transfer medium, which is returned to the beginning of the second zone, while the evaporated heat transfer medium is replaced by liquid heat transfer medium fed into the first zone from the outside.
  • reaction temperature is so low that an extremely large cooler area and thus correspondingly high investment costs would be required for heat extraction by means of steam generation via a cooler because of the small temperature difference. Nevertheless, the steam obtained in this way would be relatively inferior due to its low temperature and correspondingly low voltage.
  • the invention is intended to remedy this. It is therefore based on the task of a rationally working jacket reactor for exothermic gas phase reaction processes under moderately low, but at least to maintain the temperature exactly at the beginning.
  • the first reaction zone as an evaporation zone
  • a very precisely controllable temperature must be maintained at the beginning of the reaction, but above all even at extremely high heating surface loads over the entire cross section of the tube bundle.
  • a cooler together with a circulation pump - a relatively repair and maintenance-intensive component.
  • the resulting steam normally water vapor, can be removed immediately and is accordingly high-tensioned and therefore thermodynamically valuable. With its pressure, its temperature and thus also the temperature of the two-phase mixture in the reaction zone in question can be controlled very precisely in a simple manner.
  • both zones can consciously communicate with each other.
  • the heat transfer medium can be fed in to replace the steam removed from the first reaction zone via the subsequent zone, in order to simultaneously heat up the heat transfer medium fed in, while the post-reaction zone in question, in particular toward the reaction gas outlet, is intensively cooled by the heat transfer medium fed in there.
  • FIG. 1 schematically in longitudinal section - an embodiment of a jacket tube reactor according to the invention with a first so-called evaporation zone in relation to the process gas flow and a subsequent after-reaction zone working with heat transfer medium, including connected components, shown here only in the form of a circuit diagram,
  • Fig. 3 shows a similar tubular reactor etc. as shown in Fig. 2, but with one on the second, i.e. Post-reaction zone following post-cooling zone, through which the heat carrier feed takes place in this case, and
  • Fig. 4 is an external view of a four-zone jacket tube reactor according to the invention with subsequent components, the first reactor zone being a preheating zone for the incoming process gas and the last one being a cooling zone for the exiting process gas.
  • the jacket tube reactor 2 shown in FIG. 1 has an upright cylindrical reactor jacket 4 which surrounds a hollow-cylindrical reaction tube bundle 6, which is indicated here only by outer and inner dashed lines.
  • the tube bundle 6 extends, sealed there, between two tube plates 8 and 10.
  • the tube plates 8 and 10 are covered by a gas inlet hood 12 or a gas outlet located here.
  • Covered hood 14 for the process gas supplied via pipe socket 16 and 18 spanned, which reacts in the tubes of the tube bundle 6 by means of a catalyst filling located therein.
  • the tubes inside the reactor jacket 4 are surrounded by an essentially liquid heat transfer medium which releases the excess heat absorbed by the tubes to the outside.
  • the heat transfer medium is usually circulated by means of a circulation pump, such as the circulation pump 20 shown here, on the one hand through the reactor jacket, and on the other hand through a cooler, such as the cooler 22 shown here, in which water vapor is obtained from the heat given off there.
  • a turbulent flow of heat transfer medium at least a substantial part of the tubes interspersed with alternating annular and disk-shaped baffle plates, such as that, within the reactor jacket 4 Deflection plates 24 and 26 shown here are provided, which, however, have through-openings (so-called partial flow openings) of variable cross-section for the purpose of a desired flow distribution over the reactor cross-section around the tubes and / or between the tubes and, if appropriate, can also serve to support the tubes against vibrations.
  • the cooler can, as shown here, be arranged in a valve-controlled shunt circuit to the main heat transfer circuit including the circulating pump 20 and the reactor 2, so as to be able to control the amount of heat to be removed via the cooler and thus the process temperature occurring in the reactor.
  • the heat transfer medium is drawn off and supplied to the reactor via ring channels on the reactor jacket 4. All of these measures are common nowadays to achieve desirable process temperature control, etc.
  • a first reaction zone I is operated with evaporative cooling with respect to the process gas passing through the reactor 2, while a subsequent second reaction zone II operates in a conventional manner with circulation cooling.
  • Both zones, I and II are separated from one another by a partition plate 28, just as the two cooling systems are separated from one another.
  • the tube sheets and the reactor jacket have to be relatively strong, while the ring channels, here the ring channels 30, 32, 34 and 36, as shown, are conveniently placed inside the reactor jacket where they are not exposed to any significant pressure differential. Accordingly, the ring channels, as shown here with the help of the ring channel 30, in contrast to conventional ring channels, can be continuously open to the inside of the jacket all around.
  • the resulting steam in the reaction zone I is fed as a steam-water mixture via risers 38, which must be correspondingly voluminous, to a steam drum 40 arranged above the reactor 2, from where it passes through a continuously Steam line 44 containing controllable valve 42 is emitted, for example, to a normal steam system.
  • the vapor pressure and thus also the heat transfer medium temperature prevailing in the entire reaction zone I can be controlled very precisely via the valve 42.
  • the water deprived of its steam component in the steam drum 40 flows back into the reactor jacket 4 via the downpipes 46 and the annular channel 32. The cycle is maintained solely by gravitation, in that the steam portion in the heat carrier rising through the lines 38 drives it upward due to its correspondingly lower specific weight.
  • the heat carrier emitted by the steam drum 40 as steam is continuously replaced by feed water fed into the steam drum via a feed line 48. There, this can be preheated by means of a part of the separated steam, which condenses in the process.
  • the feed water can be sprayed in a known manner via an injection device (not shown) in order to avoid partial cooling of the water entering the downpipe 46.
  • a separate separator in the simplest case consisting of one or more baffle plates, can also be provided in the steam drum 40 for complete vapor separation from the liquid phase. Corresponding designs of a steam drum are well known and therefore do not need to be described further here.
  • both reaction zones I and II can, if desired, with different heat carriers operate. Normally, however, you will choose the same heat transfer medium, especially water, the steam of which is then also immediately, if necessary after throttling, can be supplied to a normal steam system.
  • reaction zone I part of the steam-water mixture occurring in the first reaction zone I initially serves to rapidly heat the incoming reaction gas to the reaction temperature.
  • reaction zone I By designing reaction zone I as an evaporation zone, optimal cooling with very precise temperature control can then be achieved at the beginning of the reaction where it is most violent.
  • reaction zone II even if the same heat transfer medium is used there, a lower temperature, but also a temperature gradient towards the process gas outlet can be set by the heat transfer medium conveyed via the circulation pump 20 being cooled accordingly by the partial flow conveyed via the cooler 22 becomes. This mode of operation in zone II is possible even if the two zones I and II communicate with one another on the heat carrier side, as explained below with reference to FIG. 2.
  • Fig. 2 shows a substantially like the reactor 2 of Fig. 1 designed reactor 60 with the basic difference that here the two heat transfer circuits are deliberately connected to each other via a line 62 leading from the inlet side of the circulation pump 20 into a riser 38 and the Reaction zone I of heat carriers lost due to evaporation is replaced by heat carriers fed into the heat carrier circuit of reaction zone II via a feed line 64, more precisely before or — as shown in broken lines — behind the circulating pump 20.
  • the heat carrier fed in this way contributes to cooling in zone II, while it heats itself up in a desirable manner.
  • a high temperature is Difference in tur avoided and hypothermia of the heat carrier returned from there through line 46 excluded.
  • ring channels such as the inner ring channels 30 and 32 shown in FIG. 1 can be dispensed with in zone I, if desired, by supplying and removing heat carrier to and from the reactor jacket 4 in zone I via the Ring-shaped pipelines 66 and 68 surrounding the reactor jacket take place, which are connected to the inside of the jacket via a plurality of radial connecting pipe connections 70 and 72 distributed all around.
  • the pipes 66 and 68 and the pipe sockets 70 and 72 are expediently of circular cross-section for reasons of pressure resistance. If necessary, they can, as shown in the pipe socket 70, contain throttling points 73 for more precise flow distribution.
  • FIG. 2 it is also shown in FIG. 2 how the separating plate 28 for compensating for different thermal expansions of the reactor jacket 4 and the tube bundle 6 is suspended from the reactor jacket by means of an expansion compensator 74 in the form of a bent sheet metal ring and how an annular saving line 76 is connected to the separating plate 28 Feed of steam can be arranged.
  • the latter is particularly useful for preheating Zone I in the start-up phase of the reactor before the reaction starts.
  • the tubes of the tube bundle 6 are stabilized against vibrations by a support plate, a support grate or the like. 78 supported, but without the tion of the heat transfer medium to significantly hinder. Then the ring channels 34 and 36 of the reaction zone II according to FIG. 2 are connected to the inside of the jacket via a plurality of axially superimposed window openings 80 in order to bring about a desired flow distribution.
  • the reactor 90 from FIG. 3 differs from the reactor 60 from FIG. 2 primarily in that a cooling zone III follows the second reaction zone II which works with circulation cooling.
  • a cooling zone III follows the second reaction zone II which works with circulation cooling.
  • the tubes inside the cooling zone III will normally not contain any catalyst filling. They can be filled with inert material, especially if they form immediate continuations of the reaction tubes, or also contain any metallic or ceramic internals known per se in tube coolers, such as, for example, wire helix, ceramic body or the like. to favor turbulent gas flow.
  • the cooling zone III is flanged to the reaction zone II.
  • the tubes of the cooling zone III are separated from the reaction tubes of the reaction zones I and II by two relatively closely adjacent tube sheets 92 and 94. Accordingly, their number, their diameter and their division can also differ from those of the reaction tubes and even the jacket diameters can be different. Such an aftercooler often contains fewer pipes than the actual reactor. If, however, the tubes of the cooling zone III form direct continuations of the reaction tubes, the zones II and III can be separated from one another by a partition plate similar to the partition plate 28. In the example of FIG.
  • the heat transfer medium is fed into the cooling zone III, via an injector pump 96, in which the heat transfer medium that is fed in is simultaneously heated before it reaches the heat transfer medium circuits of the reaction zones I and II from the cooling zone.
  • the injector pump 96 is operated with a partial quantity of the heat carrier leaving the cooling zone III which can be controlled via a valve 98.
  • the injector pump can be omitted, as on the other hand it can also be replaced by a mechanical pump similar to the circulation pump 20.
  • a heat exchanger, in particular a cooler, 99 can also be connected upstream of the heat transfer medium into the cooling zone III, as shown.
  • the heat carrier supplied via cooling zone III enters the circuit of zone II in the example of FIG. 3 on the inlet side of circulation pump 20, for example where line 62 to zone I also connects.
  • a valve-controllable bypass 100 which is connected in parallel with the cooler 22, can also be seen in the heat transfer circuit of zone II, as is described in detail in PCT application PCT / EP02 / 14189 dated 12.12.2002.
  • Such a bypass should, above all, allow a constant pump output of the circulating pump combined with constant flow conditions in the reactor, regardless of the amount of heat to be dissipated via the cooler 22.
  • the partial heat flows through the cooler 22 and the bypass 100 can be controlled alternately via a common three-way valve 102.
  • FIG. 3 now also shows annular pipelines 104 and 106 running around the reactor jacket 4 within the reaction zone II, in addition to the term inner ring channels 34 and 36.
  • the pipes 104 and 106 which, like the connecting pipe connections 108 and 110 which follow, can have an adapted cross section, serve to even out the inflow and outflow of the heat transfer medium.
  • Similar annular pipelines, 112 and 114, are also provided on cooling zone III, in addition to the internal annular channels 116 and 118.
  • the heat transfer medium enters and exits the annular ducts 34 and 36 via these downstream or upstream annular distribution ducts 120 and 122, which also lie within the reactor jacket 4, and which are connected to the annular ducts 34 and 36 communicate via throttle openings 124 and 126, respectively.
  • FIG. 3 a heat-insulating coating 128 of the separating plate 28 is shown in zone I, in addition to the sparger line 76 from FIG. 2.
  • the reactor 130 shown in FIG. 4 differs from the reactor 90 according to FIG. 3, apart from the lack of some optional details such as the bypass 100, essentially in that in front of the first reaction zone I there is still one Preheating zone IV is provided for the process gas entering the reactor.
  • Preheating zone IV is provided for the process gas entering the reactor.
  • the temperature profile of the heat transfer medium that can be achieved therein along the reactor length L is shown diagrammatically.
  • the temperature in the heat transfer medium in zone IV increases continuously from an initial value T **. at the inlet of the process gas to a value T 2 slightly below the constant temperature T 3 of the evaporation zone I, where the reaction begins and immediately takes place most violently, with the greatest heat.
  • Zone IV in turn has a heat transfer roller system, which however supplies heat to the process gas stream.
  • a heat exchanger 134 within the steam drum 40 heats up heat transfer medium - the same as or different than in zones I to III - via an annular channel 136 at the gas outlet end of zone IV and enters the reactor jacket 4 and via an annular channel 138 at the gas inlet end of zone IV in order to move globally in countercurrent to the process gas stream.
  • the contact tubes of the tube bundle 6 can pass through the zone IV, in which case the zone IV is separated from the zone I by a partition plate similar to the partition plate 28.
  • zones IV and I can be separated from one another by adjacent tube sheets, in which case zones IV and I can have different tube diameters and / or arrangements - which, however, should rarely be used.
  • the tubes within zone IV apart from the process gas may be empty, have a catalyst or inert material filling, contain turbulence-promoting internals and the like. more like the pipes inside the cooling zone III.
  • the partial flow of the heat carrier of zone IV leading via the heat exchanger 134 can be controlled by a valve 140.
  • the heat transfer Zones I to III can, but need not, as shown, be connected.
  • the supply for replacing the heat carrier lost through evaporation can be carried out according to FIG. 3 via the cooling zone III, in the latter case it must take place, as shown in FIG. 1, for example via the steam drum 40, into the heat carrier circuit of the evaporation zone I.
  • a separate preheating zone such as zone IV shown in FIG. 4, is dispensed with.
  • the process gas is preheated by the heat transfer medium there when it enters zone I, for which purpose a steam cushion underneath the tube sheet 8 there (FIG. 1) can serve.
  • the global flow of heat transfer medium in the individual zones does not have to be entirely opposite to the process gas flow.
  • the process gas stream itself can also, in contrast to the exemplary embodiments described above, pass through the reactor from bottom to top.
  • the gas flow from top to bottom in connection with the invention deserves preference, since the steam drum will generally be arranged - laterally or in the middle - above the reactor and the naturally voluminous risers to it - like the risers 38 according to FIG. 1 - expediently be kept short.
  • circulation pumps and coolers can generally be arranged on the floor in order to counteract a tendency to cavitation.
  • reaction zones I and II can be joined by further reaction zones working with or without evaporative cooling, and the like. more.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

L'invention concerne un réacteur tubulaire à enveloppe (2 ; 60 ; 90 ; 130) comprenant plusieurs zones et servant à exécuter des réactions exothermiques en phase gazeuse. Le réacteur tubulaire à enveloppe selon l'invention comprend au moins une zone de réaction (I) fonctionnant en refroidissement par évaporation, au moins une zone de réaction (II) fonctionnant en refroidissement par circulation et, éventuellement, d'autres zones (III, IV). Le réacteur tubulaire à enveloppe selon l'invention est caractérisé en ce qu'une zone de réaction (I) fonctionnant en refroidissement par évaporation constitue la première zone de réaction, à laquelle se raccorde une autre zone de réaction fonctionnant en refroidissement par évaporation ou une zone de réaction (II) fonctionnant en refroidissement par circulation. On obtient ainsi, au début de la réaction où cette dernière est la plus violente, un refroidissement très intensif avec une température qui peut être pilotée de manière précise et qui est surtout constante sur toute la section du réacteur, alors qu'on obtient ensuite un refroidissement progressif du gaz de réaction dans une zone de réaction secondaire fonctionnant en refroidissement par circulation grâce à une alimentation à contre-courant globale de l'agent caloporteur.
EP03701548A 2003-01-31 2003-01-31 Reacteur tubulaire a enveloppe comprenant plusieurs zones pour l'execution de reactions exothermiques en phase gazeuse Withdrawn EP1590076A1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2003/000978 WO2004067165A1 (fr) 2003-01-31 2003-01-31 Reacteur tubulaire a enveloppe comprenant plusieurs zones pour l'execution de reactions exothermiques en phase gazeuse

Publications (1)

Publication Number Publication Date
EP1590076A1 true EP1590076A1 (fr) 2005-11-02

Family

ID=32798698

Family Applications (1)

Application Number Title Priority Date Filing Date
EP03701548A Withdrawn EP1590076A1 (fr) 2003-01-31 2003-01-31 Reacteur tubulaire a enveloppe comprenant plusieurs zones pour l'execution de reactions exothermiques en phase gazeuse

Country Status (7)

Country Link
US (1) US20070036697A1 (fr)
EP (1) EP1590076A1 (fr)
JP (1) JP2006513839A (fr)
KR (1) KR100679752B1 (fr)
CN (1) CN1738677B (fr)
AU (1) AU2003202596A1 (fr)
WO (1) WO2004067165A1 (fr)

Cited By (7)

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DE102007024934A1 (de) 2007-05-29 2008-12-04 Man Dwe Gmbh Rohrbündelreaktoren mit Druckflüssigkeitskühlung
DE102010014642A1 (de) 2010-04-12 2011-10-13 Man Diesel & Turbo Se Temperiervorrichtung und Verfahren zum Temperieren eines Rohrbündelreaktors
DE102010014643A1 (de) 2010-04-12 2011-10-13 Man Diesel & Turbo Se Rohrbündelreaktor
WO2012095356A1 (fr) 2011-01-11 2012-07-19 Bayer Materialscience Ag Procédé de production d'amines aromatiques
EP2653461A1 (fr) 2012-04-16 2013-10-23 Bayer MaterialScience AG Procédé de départ amélioré de la réaction lors de la fabrication d'amines aromatiques à partir de nitro-aromates
EP2653462A1 (fr) 2012-04-16 2013-10-23 Bayer MaterialScience AG Procédé de départ amélioré de la réaction lors de la fabrication d'amines aromatiques à partir de nitro-aromates
WO2021037990A1 (fr) 2019-08-30 2021-03-04 Covestro Deutschland Ag Procédé d'hydrogénation de composés nitroaromatiques

Families Citing this family (13)

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Publication number Priority date Publication date Assignee Title
DE102005001952A1 (de) * 2005-01-14 2006-07-27 Man Dwe Gmbh Rohrbündelreaktor zur Durchführung exothermer oder endothermer Gasphasenreaktionen
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JP5239997B2 (ja) * 2008-03-31 2013-07-17 三菱化学株式会社 プレート式反応器における温度制御方法及び反応生成物の製造方法
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WO2013156409A1 (fr) 2012-04-16 2013-10-24 Bayer Materialscience Ag Procédé d'arrêt amélioré de la réaction lors de la préparation d'amines aromatiques à partir d'aromatiques nitrés
WO2013156410A1 (fr) 2012-04-16 2013-10-24 Bayer Materialscience Ag Procédé de démarrage amélioré de la réaction lors de la préparation d'amines aromatiques à partir d'aromatiques nitrés
WO2021037990A1 (fr) 2019-08-30 2021-03-04 Covestro Deutschland Ag Procédé d'hydrogénation de composés nitroaromatiques

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WO2004067165A1 (fr) 2004-08-12
KR20050097965A (ko) 2005-10-10
CN1738677A (zh) 2006-02-22
JP2006513839A (ja) 2006-04-27
US20070036697A1 (en) 2007-02-15
KR100679752B1 (ko) 2007-02-06
AU2003202596A1 (en) 2004-08-23

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