US3566961A - Tubular reactor for carrying out endothermic and exothermic reactions with forced circulation - Google Patents

Tubular reactor for carrying out endothermic and exothermic reactions with forced circulation Download PDF

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Publication number
US3566961A
US3566961A US757957A US3566961DA US3566961A US 3566961 A US3566961 A US 3566961A US 757957 A US757957 A US 757957A US 3566961D A US3566961D A US 3566961DA US 3566961 A US3566961 A US 3566961A
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United States
Prior art keywords
reactor
tubes
orifices
plates
guide plate
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Expired - Lifetime
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US757957A
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English (en)
Inventor
Friedrich Lorenz
Joachim Wagner
Dieter Bettermann
Walter Mann
Johann Heinrich Walter
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BASF SE
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BASF SE
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
    • F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
    • 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
    • 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
    • B01J8/062—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 being installed in a furnace
    • 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
    • F28D7/16—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 being arranged in parallel spaced relation
    • F28D7/1607—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 being arranged in parallel spaced relation with particular pattern of flow of the heat exchange media, e.g. change of flow direction
    • 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
    • B01J2208/00106—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
    • 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
    • F28F2009/222—Particular guide plates, baffles or deflectors, e.g. having particular orientation relative to an elongated casing or conduit
    • F28F2009/226—Transversal partitions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S165/00—Heat exchange
    • Y10S165/355—Heat exchange having separate flow passage for two distinct fluids
    • Y10S165/40—Shell enclosed conduit assembly
    • Y10S165/401—Shell enclosed conduit assembly including tube support or shell-side flow director
    • Y10S165/402—Manifold for shell-side fluid

Definitions

  • the invention relates generally to apparatus for chemical plant having a nest oftubes and particularly to a reactor suita-' ble for carrying out endothermic and exothermic reactions, in the tubes of which the reaction takes place and in which a heat transfer medium impinges'on the outside of the tubes in axial direction, delivery of equal amounts to each individual tube being ensured by various constructional means.
  • Reaction apparatus of great capacity having a nestof tubes arranged around a central guide tube in which the medium flushing the tubes'iscirculated by a convey ing meanslocated in the guide tube.
  • the guide tube also contains a Heat exchanger whose connections are taken out from the apparatus in the central zone.
  • The-nest of tubes to be impinged onoften contains several thousand individual tubes'and special demands are made on their welds.
  • the use of highly ef fective catalysts in such apparatus means that thethroughput of medium to be conducted by the conveyingmeans through the central guide tube necessary to ensure conveyance of heat has to be increased considerably.
  • the heatexchange through the outer casing of the apparatus is negligibly small.
  • Heat transfer is in fact higher in the caseof tubes with transverse flow than in the case of axial flow, but the essential requirement of the same temperature of the heat transfer medium at the same point in each individualtube can only be fulfilled with an adequately uniform axial flow owing to the course of the reactionstriven for in the interior of the tubes.
  • the crosssectional area of the orifices in the guide plates may increase from the outside towards the inside.
  • Anotherf'eature of the invention may, consist in the provision of additional annular guide plates besides the guide plates which extend over the whole cross section of the nest of tubes.
  • FIG. I is a diagrammatic sectional elevation of a nested tube reactor according to this invention.
  • FIG. 2 is a section taken on the line A.-A in FIG. 1;
  • FIGS. 3 and 4 are details showing tubes surrounded by guide plates having appropriate orifices
  • FIG. 5 is a diagrammatic sectional elevation of a further embodiment of nested tube reactor according to the invention.
  • FIG. 6 is a section taken on the line B-B'in FIG. 5;
  • FIG. 7 is a partial vertical section illustrating in greater.
  • FIG. 7A is a partial horizontal section taken on the line A-A of FIG; 7;
  • FIG. 8 is a partial vertical section similar to FIG. 7 but illustrating another modificationof the nested tube arrangement passing through a different set of guide plates;
  • FIG. 9 is a partial'horizontal section similar to FIG. 7A to illustrate guide plates containing additional orifices or bores distributed between the orifices around individual tubes.
  • the nest 1 of tubes filled with. catalyst occupies almost all of the space enclosed by the castion enclosed by the casing 2, contains aplurality of orifices 10 of such dimensions that theheat transfer medium-flows at a velocity which is the same over the entire cross section of the nest of tubes, along the nest of tubes 1 to the upper guide plate 6.
  • the heat transfer medium passes through openings 12 in the casing 2 into the'upper circular line 7 and thence is returned to the cooler 3.
  • the openings 9 in the casing 2 at the level of the circular line 4 are of such size that the sum of the pressure lossesfrom flowing into the circular line and the: passage through the openings is the same for all the stream threads.
  • the heat transfer medium is distributed uniformly over the whole extent of the casing 2 and its uniform radical entryinto the nest of tubes is ensured.
  • These crossesectional dimensions derived from the measurable pressure losses also hold good for the egress of the heat transfer medium through theupper openings 12 of the casing 2 into the circular line 7.
  • the supply and withdrawal of heat transfer medium through the circular lines 4 and 7 located outside the casing 2 is particularly favorable, because the largest areas of passage between the guide plates 5 and 6 and the tube plates 8 and 14 are available for the largest amounts of heat transfer medium flowing.
  • the orifices 10 in the guide plates 5 and 6 are of such a size that the sum of the pressure losses from the transverse flow through the nest of tubes before and after passage through the guide plates 5 and 6, and the divided flow in the orifices is constant for stream threads situated farther out or farther in. Equal amounts of heat transfer medium then flow through equal areas of nestedtube cross section between the guide plates 5 and 6.
  • the distance of the guide plate 5 from the adjacent tube plate 8 may be such in a radial direction that the pressure loss of the transverse flow through the nest of tubes provided between these elements is constant for each stream thread inwards up to the orifices 10. It follows from this that this distance may have to be made different in the radial direction. Usually a greater distance is necessary at the outside than in the central region of the nest of tubes. Approximately the same result can be achieved if the tubes are arranged in such a way that the distance between them increases towards the center of the nest of tubes. In this embodiment the tube separation is smaller at the outside than in the center of the nest of tubes.
  • the orifices 10 in the guide plate 5 may be made the same size at every point of the cross section of the nest of tubes so that the flow of heat transfer medium along the tubes 13 is the same at every point. This provision for the distance between the guide plate and the upper tube plate 11 holds good in an analogous way for the egress of the heat transfer medium through the orifices 10 in the upper guide plate 6.
  • the guide plates are shaped either conically or hemispherically. Additional flat guide plates with orifices 10 may be installed in the heat exchanger over the length of the tubes between the shaped guide plates 5 and 6 in order if necessary to influence again the desired axial flow along the tubes.
  • FIGS. 3 and 4 show advantageous shapes for the orifices 10 in the guide plates 5 and 6.
  • These orifices 10 are preferably designed so that interstices are formed around the individual tubes 13 of the nest of tubes 1.
  • the size of the area of the interstice is regulated according to the position of the tube in the whole cross section of the nest of tubes so that the required pressure loss is achieved at this position.
  • the orifice is designed so that (as shown in FIG. 4) they completely surround two or more adjacent individual tubes as a group.
  • FIGS. 5, 6, 7, 7A, 8 and 9 are possible within the scope of this invention.
  • guide plates 5 and 6 occupying the whole cross section of the nest of tubes and having all the orifices of the same size, it is possible by this equalization to provide further flat guide plates 5, 5 and 6, 6 having a smaller total area and having orifices still of the same size.
  • these additional guide plates having smaller areas are constructed as annular surfaces having an appropriate number of orifices 10, the outer diameter of these guide plates being about equal to the inner diameter of the casing of the casing of the apparatus.
  • FIGS. 5 and 6 This embodiment of the reactor is shown diagrammatically in FIGS. 5 and 6 and in a more detailed vertical or horizontal section in FIGS. 7, 7A and 8.
  • the cross sections of the openings 9 at the level of the circular inlet line 4 and, correspondingly, those of the openings 12 at the level of the circular outlet line 7, in order to equalize different pressure losses on the way from the conveying means 3a to the entry into the nest of tubes, advantageously increase from entry or outlet point of the heat transfer medium into (or out from) the circular line up to the opposite side of the periphery of the casing.
  • the orifices 10, 10' and 10 are advantageously not only equal in area but of the same geometrical shape, i.e., made congruent. After the heat transfer medium has passed through the orifices of the guide plates 6, 6' and 6", it passes through openings 12 in the casing 2 into the upper circular line 7 and thence is returned to the conveying means 3a (see FIGS. 5 and 6).
  • the openings 9 in the casing 2 at the level of the circular line 4 are of such size that the sum of the pressure losses from the flow in the circular line and passage through the openings is the same for all stream threads. In this way the heat transfer medium is distributed over the whole extent of the casing 2 and its uniform radial entry into the nest of tubes is ensured. The same is true of the dimensions of the cross section derived from the measurable pressure loss for the egress of the heat transfer medium through the upper openings 12 of the casing 2 into the circular line 7.
  • the orifice 10, 10 and 10" in the guide plates 5,5 and 5" and 6, 6 and 6" are of such size that the sum of the pressure losses from the transverse flow through the nest of tubes 1 and from the flow through the orifices 10, 10 and 10" is the same for all stream threads. Equal amounts of heat transfer medium then flow through the same areas of nested tube cross section between the guide plates 5, 5 and 5" and 6,6 and 6".
  • Adaptation to the different pressure losses across the whole of the nest of tubes may also be carried out in this embodiment by varying the effective length of the orifices 10 following each other at the individual tubes. In practice this is effected, the cross-sectional areas of the orifices 10 being of equal size, by making the total thickness of all the guide plates smaller in stages from the outside towards the center.
  • the annular guide plates 5' and 5 and 6' and 6" may be provided at increasing inward distances away from each of their corresponding guide plates 5 and 6, respectively, (as shown in FIGS. 7 and 7A) or else these additional guide plates may be welded direct to the guide plates 5 and 6 (as shown in FIG. 8).
  • the stagewise reduction in the thickness of the plates is again such that the sum of the pressure losses from the transverse flow through the nest of tubes 1 and the flow through the orifices 10 is equal for all stream threads.
  • a nested tube reactor for carrying out endothermic and exothermic reactions with forced circulation of a heat transfer medium flushing the tubes from a conveying means located externally of the heat exchanger formed by the reactor tubes enclosed by a casing having inlet and outlet openings around its periphery in communication with one circular line for the supply and another circular line for the withdrawal of said heat transfer medium which is circulated by said conveying means
  • the improvement in combination therewith which comprises a perforated guide plate means arranged substantially transversely to the axes of the tubes to extend over the cross section of the reactor and containing orifices of equal size surrounding the tubes while the thickness of said guide plate means is varied from the outside to the center of the reactor to provide a corresponding variation in the effective length of the orifices such that the heat transfer medium flows uniformly over the cross section of the reactor.
  • a nested tube reactor as claimed] in claim 2 wherein said tubes are mounted at either end and held by tube plates, a fiat guide plate extending across the entire cross section of the reactor is positioned adjacent to and at an inwardly spaced distance away from each of said tube plates along the tube axes, and a plurality of additional annular flat guide plates are provided at increasing inward distances away from each of said first-named guide plates, the totall area of each additional annular guide plate associated with one of said first-named guide plates becoming progressively smaller than the preceding guide plate in a direction inwardly along the tube axes.

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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)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US757957A 1967-09-06 1968-09-06 Tubular reactor for carrying out endothermic and exothermic reactions with forced circulation Expired - Lifetime US3566961A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE1601162 1967-09-06
DE1601163 1967-09-23

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US3566961A true US3566961A (en) 1971-03-02

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US (1) US3566961A (fr)
BE (1) BE720496A (fr)
CH (1) CH493811A (fr)
CS (1) CS154594B2 (fr)
FR (1) FR1577926A (fr)
GB (1) GB1241703A (fr)
NL (1) NL6812591A (fr)
RO (1) RO59253A (fr)

Cited By (40)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3762465A (en) * 1970-12-17 1973-10-02 Deggendorfer Werft Eisenbau Arrangement of a heating unit in reaction apparatus
US3792980A (en) * 1971-08-27 1974-02-19 Veba Chemie Ag Reactor for carrying out reactions accompanied by a change in heat
US3830292A (en) * 1972-05-01 1974-08-20 Atomic Energy Commission Flow distribution for heat exchangers
US3850232A (en) * 1972-02-16 1974-11-26 Deggendorfer Werft Eisenbau Reactor cooling system with an evaporation tank
US3871445A (en) * 1972-01-13 1975-03-18 Deggendorfer Werft Eisenbau Reaction apparatus for carrying out exothermic and endothermic chemical processes with radial flow of a heat exchange medium
US3907029A (en) * 1972-09-04 1975-09-23 Siemens Ag Steam generator
US3960207A (en) * 1973-11-28 1976-06-01 Boer Karl W Heat exchange apparatus
US4120350A (en) * 1975-03-19 1978-10-17 The Babcock & Wilcox Company Tube support structure
US4256783A (en) * 1977-07-13 1981-03-17 Nippon Skokubei Kagaku Kogyo Co., Ltd. Catalytic vapor phase oxidation reactor apparatus
US4303618A (en) * 1978-11-27 1981-12-01 Kawasaki Jukogyo Kabushiki Kaisha Catalytic reactor
US4305458A (en) * 1978-06-22 1981-12-15 Patrick Jogand Reactors in which the cooling of the core is brought about by the continuous circulation of a liquid metal
US4397768A (en) * 1981-02-26 1983-08-09 Oxidaciones Organicas, C.A. "Oxidor" Supported catalyst for the preparation of phthalic anhydride
US4635707A (en) * 1982-07-06 1987-01-13 Phillips Petroleum Company Method for varying shell fluid flow in shell and tube heat exchanger
US4657741A (en) * 1984-03-13 1987-04-14 Deggendorfer Werft Und Eisenbau Gmbh Reactor construction
US4737347A (en) * 1985-07-27 1988-04-12 Metallgesellschaft Aktiengesellschaft Multi-tube reactor
US4921681A (en) * 1987-07-17 1990-05-01 Scientific Design Company, Inc. Ethylene oxide reactor
US4929798A (en) * 1984-03-05 1990-05-29 Canadian Patents And Development Limited Pseudoadiabatic reactor for exothermal catalytic conversions
US4991648A (en) * 1989-02-10 1991-02-12 Mitsubishi Jukogyo Kabushiki Kaisha Multi-tube type heat transfer apparatus
US5203405A (en) * 1992-02-03 1993-04-20 Phillips Petroleum Company Two pass shell and tube heat exchanger with return annular distributor
US5425415A (en) * 1993-06-15 1995-06-20 Abb Lummus Crest Inc. Vertical heat exchanger
US5595242A (en) * 1994-05-13 1997-01-21 Schmidt'sche Heissdampf Gmbh Heat exchanger
US5739391A (en) * 1994-09-08 1998-04-14 Basf Aktiengesellschaft Catalytic gas-phase oxidation of acrolein to acrylic acid
US5821390A (en) * 1994-09-08 1998-10-13 Basf Aktiengesellschaft Catalytic gas-phase oxidation of propene to acrolein
WO2000054877A2 (fr) * 1999-03-16 2000-09-21 Basf Aktiengesellschaft Reacteur a faisceau de tubes destine notamment a des reactions en phase gazeuse catalytique
US6384274B1 (en) 1998-09-27 2002-05-07 Rohm And Haas Company Single reactor process for preparing acrylic acid from propylene having improved capacity
US20030068261A1 (en) * 2001-08-02 2003-04-10 Hassan Taheri Flow reactors for chemical conversions with heterogeneous catalysts
US20040081609A1 (en) * 1996-04-03 2004-04-29 Green Martin C. Heat exchanger
US6747162B2 (en) 2000-05-17 2004-06-08 Basf Aktiengesellschaft Counterflow reactor with a bundle of contact tubes
US6756023B1 (en) 1998-08-13 2004-06-29 Basf Aktiengesellschaft Reactor comprising a contact tube bundle
US20040156721A1 (en) * 2001-06-06 2004-08-12 Gerhard Olbert Pump for transporting heat-exchange medium for a multi-tube reactor
US20100000707A1 (en) * 2006-10-25 2010-01-07 Kenji Tsubone Thermal storage device
US20100307726A1 (en) * 2009-06-09 2010-12-09 Honeywell International Inc. Multi-Stage Multi-Tube Shell-and-Tube Reactor
US20110009627A1 (en) * 2008-01-25 2011-01-13 Basf Se Reactor for carrying out high pressure reactions, method for starting and method for carrying out a reaction
US8969634B2 (en) 2011-09-26 2015-03-03 Honeywell International Inc. Combination reactor system
US20160003551A1 (en) * 2013-02-18 2016-01-07 Mitsubishi Hitachi Power System, Ltd. Heat exchanger and gas turbine plant provided therewith
EP2678628B1 (fr) * 2011-07-22 2017-02-01 Univerzita Karlova V Praze Lékarská Fakulta V Plzni Echangeur de chaleur avec dispositif de laminarisation
US10502451B2 (en) * 2017-05-02 2019-12-10 Rheem Manufacturing Company Diffuser plates and diffuser plates assemblies
US20220203322A1 (en) * 2020-12-30 2022-06-30 Scientific Design Company, Inc. Corrugated grid support for vertical boiling reactor
US20220236014A1 (en) * 2019-05-28 2022-07-28 Sulzer Management Ag Tube-bundle heat exchanger comprising assemblies/built-in elements formed of deflection surfaces and directing sections
US11512902B2 (en) * 2017-11-01 2022-11-29 Holtec International Flow baffles for shell and tube heat exchangers

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH527390A (de) * 1972-04-07 1972-08-31 Sulzer Ag Verdampfer

Cited By (55)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3762465A (en) * 1970-12-17 1973-10-02 Deggendorfer Werft Eisenbau Arrangement of a heating unit in reaction apparatus
US3792980A (en) * 1971-08-27 1974-02-19 Veba Chemie Ag Reactor for carrying out reactions accompanied by a change in heat
US3871445A (en) * 1972-01-13 1975-03-18 Deggendorfer Werft Eisenbau Reaction apparatus for carrying out exothermic and endothermic chemical processes with radial flow of a heat exchange medium
US3850232A (en) * 1972-02-16 1974-11-26 Deggendorfer Werft Eisenbau Reactor cooling system with an evaporation tank
US3830292A (en) * 1972-05-01 1974-08-20 Atomic Energy Commission Flow distribution for heat exchangers
US3907029A (en) * 1972-09-04 1975-09-23 Siemens Ag Steam generator
US3960207A (en) * 1973-11-28 1976-06-01 Boer Karl W Heat exchange apparatus
US4120350A (en) * 1975-03-19 1978-10-17 The Babcock & Wilcox Company Tube support structure
US4256783A (en) * 1977-07-13 1981-03-17 Nippon Skokubei Kagaku Kogyo Co., Ltd. Catalytic vapor phase oxidation reactor apparatus
US4305458A (en) * 1978-06-22 1981-12-15 Patrick Jogand Reactors in which the cooling of the core is brought about by the continuous circulation of a liquid metal
US4303618A (en) * 1978-11-27 1981-12-01 Kawasaki Jukogyo Kabushiki Kaisha Catalytic reactor
US4397768A (en) * 1981-02-26 1983-08-09 Oxidaciones Organicas, C.A. "Oxidor" Supported catalyst for the preparation of phthalic anhydride
US4635707A (en) * 1982-07-06 1987-01-13 Phillips Petroleum Company Method for varying shell fluid flow in shell and tube heat exchanger
US4929798A (en) * 1984-03-05 1990-05-29 Canadian Patents And Development Limited Pseudoadiabatic reactor for exothermal catalytic conversions
US4657741A (en) * 1984-03-13 1987-04-14 Deggendorfer Werft Und Eisenbau Gmbh Reactor construction
US4737347A (en) * 1985-07-27 1988-04-12 Metallgesellschaft Aktiengesellschaft Multi-tube reactor
US4921681A (en) * 1987-07-17 1990-05-01 Scientific Design Company, Inc. Ethylene oxide reactor
US4991648A (en) * 1989-02-10 1991-02-12 Mitsubishi Jukogyo Kabushiki Kaisha Multi-tube type heat transfer apparatus
US5203405A (en) * 1992-02-03 1993-04-20 Phillips Petroleum Company Two pass shell and tube heat exchanger with return annular distributor
US5425415A (en) * 1993-06-15 1995-06-20 Abb Lummus Crest Inc. Vertical heat exchanger
US5595242A (en) * 1994-05-13 1997-01-21 Schmidt'sche Heissdampf Gmbh Heat exchanger
US5739391A (en) * 1994-09-08 1998-04-14 Basf Aktiengesellschaft Catalytic gas-phase oxidation of acrolein to acrylic acid
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Also Published As

Publication number Publication date
FR1577926A (fr) 1969-08-08
RO59253A (fr) 1976-02-15
GB1241703A (en) 1971-08-04
NL6812591A (fr) 1969-03-10
CS154594B2 (fr) 1974-04-30
CH493811A (de) 1970-07-15
BE720496A (fr) 1969-03-06

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