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EP1148940A1 - Module reacteur a faisceau de tubes de contact - Google Patents

Module reacteur a faisceau de tubes de contact

Info

Publication number
EP1148940A1
EP1148940A1 EP99965470A EP99965470A EP1148940A1 EP 1148940 A1 EP1148940 A1 EP 1148940A1 EP 99965470 A EP99965470 A EP 99965470A EP 99965470 A EP99965470 A EP 99965470A EP 1148940 A1 EP1148940 A1 EP 1148940A1
Authority
EP
European Patent Office
Prior art keywords
reactor
heat exchange
exchange medium
reactor module
prechamber
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Withdrawn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
EP99965470A
Other languages
German (de)
English (en)
Inventor
Gerhard Olbert
Franz Corr
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.)
BASF SE
Original Assignee
BASF SE
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 BASF SE filed Critical BASF SE
Publication of EP1148940A1 publication Critical patent/EP1148940A1/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Withdrawn legal-status Critical Current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
    • 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
    • B01J19/2425—Tubular reactors in parallel
    • 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
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • 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
    • F28D7/0058—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 the conduits for only one medium being tubes having different orientations to each other or crossing the conduit for the other heat exchange medium
    • 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
    • F28F9/26—Arrangements for connecting different sections of heat-exchange elements, e.g. of radiators
    • 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
    • B01J2219/00002—Chemical plants
    • B01J2219/00018—Construction aspects
    • B01J2219/0002—Plants assembled from modules joined together
    • 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
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00094—Jackets
    • 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
    • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
    • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor

Definitions

  • the invention relates to a reactor module with a contact tube bundle, a reactor made up of two or more reactor modules arranged in a row, and the use of a reactor module or a reactor for carrying out oxidation reactions.
  • the usual design of generic reactors consists of a, usually cylindrical, container in which a bundle, i.e. a plurality of contact tubes is usually arranged in a vertical arrangement.
  • These contact tubes which may contain supported catalysts, are sealed with their ends in tube sheets and each open into a hood connected to the container at the upper or lower end.
  • the reaction mixture flowing through the catalyst tubes is supplied or discharged via these hoods.
  • a heat exchange medium circuit is passed through the space surrounding the contact tubes in order to balance the heat balance, in particular in the case of reactions with a strong exotherm.
  • reactors with the largest possible number of contact tubes are used, the number of contact tubes accommodated often being in the range from 10,000 to 40,000 (cf. DE-A-44 31 949).
  • the cylindrical reactor geometry has the disadvantage that, in particular in the technologically particularly advantageous crossflow of the heat exchange medium to the contact tubes from an area outside the contact tubes to the contact tube-free interior of the reactor, the radially inwardly decreasing cross-sectional area does not allow the full coolant flow to the inside of the contact tube bundle. Rather, coolant must be removed axially through bores in the baffle plates in order to keep the pressure loss and thus the pump output within acceptable limits.
  • the object of the invention is to provide a reactor whose capacity can be adapted to the requirements of the individual case.
  • the solution is based on a reactor module with a contact tube bundle, through the space surrounding the contact tubes of which a heat exchange medium circuit is led with supply and discharge lines at both ends of the reactor module with jacket openings for the supply and discharge of a heat exchange medium in cross flow to the contact tubes by means of a or several pumps, if necessary by transferring the heat exchange medium or a partial flow of the heat exchange medium via one or more external heat exchangers, the heat exchange medium being fed to the lower line and being returned to the pump (s) via the upper line.
  • the solution is then characterized in that the reactor module has a rectangular cross section.
  • a hood delimiting a pressurized gas space can also be designed in a semi-cylindrical geometry, as used for both sides of a container with a rectangular cross-section is necessary.
  • Contact tube-free spaces are preferably arranged in the reactor space on two opposite reactor side surfaces parallel to the contact tubes, which preferably extend over the entire reactor height, and one or more baffle plates which alternately leave average cross sections in the contact tube-free spaces.
  • the contact tube-free spaces are preferably arranged on the two wide reactor side surfaces.
  • a ratio of 1: 1 to 10: 1 is advantageous, preferably from 3: 1 to 6: 1, particularly preferably from 5: 1. Relative values of 1.5 m to 7 m are preferred for the reactor height.
  • An odd number of deflection plates is preferably provided; this means that the heat exchange medium is supplied and removed on the same side of the reactor module. 1, 3 or 5 deflection plates are particularly preferably provided.
  • a particularly space-saving arrangement is thus achieved.
  • Different heat profiles may be required due to the course of the reaction; an adaptation to the requirements of the individual case is possible in that the heat exchange medium flow is adapted by means of one or more bypasses through the deflection plates in their tube-free areas, with fixed or controllable through openings.
  • a particularly preferred embodiment variant is a reactor module with intermediate walls in the supply and discharge lines, which each form a lower outer prechamber and a lower inner prechamber in the feed line and an upper outer prechamber and an upper inner prechamber in the discharge line.
  • the heat exchange medium becomes the lower outer prechamber, via an area between the supply line and the discharge line of the upper inner prechamber, via its jacket opening to the reactor chamber surrounding the contact tubes, then via a jacket opening of the lower inner antechamber, via the area between the supply and discharge lines of the upper outer chamber and finally returned via the discharge line to the pump (s).
  • an adaptation to the respectively required temperature profile can be achieved by an outer chamber adjacent to the wide reactor side assigned to the contact tube-free space with openings to the reactor space surrounding the contact tube bundle and with fixed or controllable through openings for the heat exchange medium in the outer chamber.
  • a particularly advantageous embodiment provides for a pipe division, according to which the contact tubes of the contact tube bundle are arranged in rows which are offset with respect to one another, the ratio of the tube distance s q transversely to the direction of flow through the heat exchange medium to the tube distance s longitudinally to the direction of flow through the heat exchange medium preferably being greater than or equal to 2 • V3, particularly preferably equal to 2 • 3.
  • Such a tube arrangement opposes the inflowing heat exchange medium with a lower resistance; the pressure loss is correspondingly lower with a higher heat transfer coefficient.
  • the invention also relates to a reactor which is constructed from two or more reactor modules arranged in a row in the direction of the longitudinal axis of the contact tube and on the narrow side surfaces.
  • Such reactors are characterized through a flexible capacity that can be adapted to the specific requirements.
  • the semi-cylindrical hoods that close the gas space can be extended to one of their flat side surfaces, which are provided with through openings accordingly. An upper limit for the capacity of reactors is thus lifted.
  • the heat exchange medium circuit can be used for the removal as well as the supply of heat from or to the reaction mixture flowing through the contact tubes; the reactor module according to the invention or the reactor according to the invention can thus be used for both exothermic and endothermic reactions. They are particularly suitable for carrying out oxidation reactors, in particular for the preparation of phthalic anhydride, maleic anhydride, glyoxal, (meth) acrolein or (meth) acrylic acid.
  • FIG. 1 shows a schematic illustration of a reactor module according to the invention
  • FIG. 2 shows a longitudinal section through a reactor module according to the invention
  • FIG. 3 shows a longitudinal section through a preferred embodiment of a reactor module according to the invention
  • FIG. 4 shows a longitudinal section through a further preferred embodiment of a reactor module according to the invention
  • Figure 5 shows a preferred arrangement of the contact tubes
  • FIG. 6 shows a reactor constructed by way of example from three reactor modules.
  • Figure 1 shows a reactor module 1 with a rectangular cross section with a vertical contact tube bundle 2, with feed line 3 and discharge line 4 for the heat exchange medium and with jacket openings 5, 6 to the reactor module 1.
  • On the opposite wide side surfaces of the reactor module there are contact tube-free spaces 7, 8 for Distributing or collecting the heat exchange medium provided.
  • the baffles 9 cause fflef '-shaped guide the heat exchange medium.
  • the gas or gas mixture G is introduced into the gas inlet space 21, flows through the contact tubes 2 and is then discharged via the gas outlet collector 22. Pumps P and heat exchanger W are arranged on the same wide side of the reactor module 1.
  • bypasses for the flow of heat exchange medium are additionally shown in the baffle plates 9, in their contact tube-free regions, which open controllable through openings 10 or through openings 11 for the heat exchange medium.
  • FIG. 3 shows a longitudinal section through a preferred embodiment variant, with direct current flow of heat exchange medium and gas mixture G.
  • a lower outer prechamber 13, a lower inner prechamber 14 and an upper outer prechamber 15 are provided by means of partition walls 12 in the supply and discharge lines 3, 4 and an upper inner prechamber 16 is formed.
  • the heat exchange medium is then fed from the feed line 3 into the lower outer prechamber 13, via a region between the feed and discharge lines 3, 4 of the upper inner prechamber 16, via the jacket opening 5 to the space surrounding the contact tubes and then via the jacket opening 6 , the lower inner prechamber 14, an area between the supply and discharge lines 3, 4 and the upper outer prechamber 15 to the pump (s).
  • an outer chamber 17 can be arranged on the divided antechambers 13 to 16 opposite the wide reactor outside, with openings 18, 19 to the reactor module or to the space 8 free of contact tubes or adjustable passage openings 20 can be set.
  • one or more heat exchangers W are arranged on the wide side of the reactor module 1 opposite the pump (s), via which partial flows of the heat exchange medium are conducted out of the contact tube-free space 8.
  • Figure 5 shows a cross section through a reactor module with a particularly favorable
  • Pipe arrangement The pipes are then arranged in rows offset from one another, the sealing distance s q transverse to the flow direction through the heat exchange medium to the pipe distance si longitudinal to the flow direction through the
  • Heat transfer media are in a ratio of 2 • V3.
  • the pipe distance s_ diagonally to the flow direction through the heat exchange medium is smaller than the pipe distance s q .
  • FIG. 6 shows an example of a reactor constructed by lining up three reactor modules 1. All pumps P and heat exchanger W are arranged on the same side of the reactor modules in a space-saving manner.
  • the invention ensures a constant flow of heat exchange medium over the reactor cross section. As a result, a uniform heat transfer coefficient to the reaction mixture flowing through the contact tubes and thus advantageous reaction control are achieved.
  • the design according to the invention reduces the pressure loss by up to half compared to conventional designs. This improves economy, since lower pump capacities or higher amounts of heat exchange medium are possible.
  • a further reduction in pressure loss is achieved through the particularly favorable, offset pipe division with the narrowest cross-section in the diagonal to the flow direction through the heat exchange medium.
  • Another advantage of the device according to the invention is its modular design, that is to say that reactors with any capacity can be made available by stringing together a corresponding number of reactor modules.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Details Of Heat-Exchange And Heat-Transfer (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un module réacteur (1) comportant un faisceau de tubes de contact (2). A travers l'espace entourant les tubes de contact passe un circuit de milieu d'échange thermique comportant des canalisations d'amenée et d'évacuation (3, 4) situées aux deux extrémités du module réacteur (1), ce dernier présentant une section rectangulaire. Des modules réacteurs (1) peuvent être montés en série en nombre quelconque et ainsi être accouplés pour former des réacteurs de capacité souhaitée.
EP99965470A 1998-12-15 1999-12-15 Module reacteur a faisceau de tubes de contact Withdrawn EP1148940A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE1998157842 DE19857842A1 (de) 1998-12-15 1998-12-15 Reaktormodul mit einem Kontaktrohrbündel
DE19857842 1998-12-15
PCT/EP1999/009971 WO2000035574A1 (fr) 1998-12-15 1999-12-15 Module reacteur a faisceau de tubes de contact

Publications (1)

Publication Number Publication Date
EP1148940A1 true EP1148940A1 (fr) 2001-10-31

Family

ID=7891160

Family Applications (1)

Application Number Title Priority Date Filing Date
EP99965470A Withdrawn EP1148940A1 (fr) 1998-12-15 1999-12-15 Module reacteur a faisceau de tubes de contact

Country Status (5)

Country Link
EP (1) EP1148940A1 (fr)
JP (1) JP2002532224A (fr)
CN (1) CN1330571A (fr)
DE (1) DE19857842A1 (fr)
WO (1) WO2000035574A1 (fr)

Families Citing this family (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10000584A1 (de) * 2000-01-10 2001-07-12 Basf Ag Verfahren zur katalytischen Gasphasenoxidation zu Maleinsäureanhydrid
AU2001235405A1 (en) * 2000-01-10 2001-07-24 Basf Aktiengesellschaft Method for catalytic gas phase oxidation to produce phthalic acid anhydride
DE10127365A1 (de) 2001-06-06 2002-12-12 Basf Ag Pumpe zur Förderung eines Wärmetauschmittels für einen Kontaktrohrbündelreaktor
KR100450234B1 (ko) * 2002-07-10 2004-09-24 주식회사 엘지화학 개선된 열교환 시스템을 갖는 촉매 산화 반응기
WO2004052526A1 (fr) * 2002-12-12 2004-06-24 Man Dwe Gmbh Reacteur tubulaire a enveloppe dote d'une derivation pour le caloporteur
CN102759298A (zh) * 2012-07-25 2012-10-31 西安交通大学 一种换热器管束的布置方式
CN112090388B (zh) * 2020-09-07 2022-04-12 浙江大学 一种连续流反应器及其在化学反应和合成中的应用

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2120538A (en) * 1920-10-22 1938-06-14 American Cyanamid & Chem Corp Process of oxidizing naphthalene to phthalic anhydride
FR1136370A (fr) * 1954-11-05 1957-05-13 Combustion Eng Perfectionnements apportés aux appareils pour transmettre de la chaleur d'un gaz àun autre à travers des parois métalliques
BE795180A (fr) * 1972-02-16 1973-05-29 Deggendorfer Werft Eisenbau Groupe refroidisseur destine a des appareils pour la realisation de reactions chimiques exothermiques

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO0035574A1 *

Also Published As

Publication number Publication date
WO2000035574A1 (fr) 2000-06-22
DE19857842A1 (de) 2000-06-21
CN1330571A (zh) 2002-01-09
JP2002532224A (ja) 2002-10-02

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