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EP1251952A1 - Reacteur a echange thermique - Google Patents

Reacteur a echange thermique

Info

Publication number
EP1251952A1
EP1251952A1 EP01900171A EP01900171A EP1251952A1 EP 1251952 A1 EP1251952 A1 EP 1251952A1 EP 01900171 A EP01900171 A EP 01900171A EP 01900171 A EP01900171 A EP 01900171A EP 1251952 A1 EP1251952 A1 EP 1251952A1
Authority
EP
European Patent Office
Prior art keywords
process gas
reactor
tube
header
tubes
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Withdrawn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
EP01900171A
Other languages
German (de)
English (en)
Inventor
Raymond Davies
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.)
Imperial Chemical Industries Ltd
Original Assignee
Imperial Chemical Industries Ltd
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 Imperial Chemical Industries Ltd filed Critical Imperial Chemical Industries Ltd
Publication of EP1251952A1 publication Critical patent/EP1251952A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/384—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts the catalyst being continuously externally heated
    • 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
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • 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
    • 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
    • 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
    • F28F9/02—Header boxes; End plates
    • F28F9/026—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits
    • F28F9/027—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes
    • F28F9/0275—Header boxes; End plates with static flow control means, e.g. with means for uniformly distributing heat exchange media into conduits in the form of distribution pipes with multiple branch pipes
    • 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
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases

Definitions

  • This invention relates to a heat exchange reactor for effecting endothermic reactions which may be catalytic or non-catalytic
  • a process gas for example a mixture of a hydrocarbon feedstock and steam and/or carbon dioxide
  • a catalyst for example nickel disposed on a suitable catalyst support such as alumina, zirconia or a calcium aluminate cement
  • Another type of reaction is the reforming or cracking of hydrocarbons such as ethane, propane, butane and/or naphtha to form olefins wherein the hydrocarbon feedstock, often in admixture with a diluent such as steam, is passed through tubes, which are often free of catalyst, while the tubes are strongly heated Thermal cracking of the hydrocarbon feedstock takes place to give a product gas containing a mixture of lower hydrocarbons such as ethylene and propylene
  • a typical reactor there may be 50 or more, for example 100 to 300, such tubes, each having a length of several metres, and during use the tubes are subjected to high temperatures, typically in the range 500-1100°C
  • the weight of the tubes, the high temperatures and consequent thermal expansion, and any pressure differential between the interior and exterior of the tubes present significant mechanical problems in the reactor design
  • One typical arrangement is described in US 4810472 wherein the reactor has a shell in which are mounted a plurality of reformer tubes with each reformer tube having a concentric double-tube configuration with a catalyst disposed in the annulus between an outer tube, herein termed a scabbard tube, and an inner tube, herein termed a bayonet tube
  • the scabbard tubes are closed at their lower ends so that the process gas flows down through the annulus and then up through the central bayonet tube
  • Surrounding each scabbard tube is a sheath tube so that the heating gas flows through the annulus between the sheath tube and the scabbard
  • the present invention provides a heat exchange reactor including an outer shell provided with process gas inlet and outlet ports, a plurality of reactor tubes supported at their upper ends, header means for supplying process gas from said inlet port to the upper ends of the reactor tubes, said header means including two or more primary inlet headers disposed across the upper part of said shell, each primary inlet header having a depth greater than its width whereby said tubes are supported, relative to said shell, directly or indirectly by said primary inlet headers
  • the reactor is of the aforesaid double-tube type and the shell is provided with an inlet port for a heating gas
  • the product process gas may be mixed with the heating gas so that the process gas outlet port forms the outlet port for the heating gas
  • the heating gas is not mixed with the process gas and so the shell is provided with a separate outlet port for the heating gas
  • the reactor tubes are of a single tube configuration and their lower ends are connected to the process gas outlet port by means of tailpipes connected to an outlet manifold or to a tube plate provided at the lower part of the shell to provide a process gas off-take zone with the heating gas is supplied to the region above the tube plate
  • the tubes may extend through, but are not fastened to, a tube plate defining a products off-take zone at the lower end of the shell, so that sliding movement can occur between the tubes and the tube plate to accommodate the thermal expansion of the tubes
  • a seal is generally necessary between the tubes and the tube plate, but where the heating gas is the reacted process gas after the latter has been subjected to further processing, the seal configuration described in US 5958364 may be employed In these arrangements using a tube plate at the lower part of the shell, since the tube plate does not have to carry the weight of the tubes, some of the mechanical problems associated therewith are significantly reduced
  • the reactor tubes are single tubes open at their lower ends so that the reacted process gas is discharged into the region outside the tubes
  • a further gas is introduced into the shell and with which the reacted process gas is mixed
  • the further gas may be a hot gas from another source, e g another reformer, for example as described in US 4337170, or an oxidant gas, e g air, oxygen-enriched air, or substantially pure oxygen, which is introduced to effect partial combustion, and hence heating of the reacted process gas to provide the heating gas
  • the weight of the reactor tubes is borne relative to the shell, by two or primary inlet headers extending across the upper part of the shell These primary inlet headers serve the dual purpose of carrying the weight of the reactor tubes and providing part of the conduit required to supply the process gas from the process gas inlet port to the reactor tubes
  • the primary inlet headers need to be of such size that they can carry the weight of the reactor tubes across the span of the shell, which may have a diameter of several metres without
  • the primary inlet headers support the reactor tubes directly or indirectly
  • the hollow primary inlet headers which are connected to the process gas inlet port, carry, and communicate with, a plurality of hollow secondary inlet header conduits and the reactor tubes are carried by, and communicate with, the secondary inlet header conduits
  • the outer, i e scabbard, tubes are carried by, and communicate with the secondary inlet header conduits, while the inner, i e bayonet tubes, may be supported in like fashion by the outer, scabbard, tubes and connected to primary and/or secondary outlet header conduits by non-load bearing pipes, or may be carried by such primary and/or secondary outlet header conduits In either case the primary and secondary outlet conduits are preferably supported directly or indirectly by the primary inlet headers
  • Suitable means such as bellows may be used to form a gas-tight connection between the process gas inlet and outlet ports and the primary inlet and outlet headers while still allowing movement to accommodate thermal expansion
  • Figure 1 is a diagrammatic vertical section through a reactor in accordance with the invention
  • Figure 2 is a diagrammatic plan of the reactor of Figure 1 with the upper portion of the shell removed
  • Figure 3 is an enlarged section along the line ll-ll of Figure 2
  • Figure 4 is a section along line Ill-Ill of Figure 3
  • Figure 5 is an enlarged section of the arrangement of supporting the primary inlet headers relative to the shell in an alternative embodiment
  • the reactor comprises an outer shell having an upper section 10 and a lower section 1 1
  • Each section has a lining of refractory insulation 12, 13
  • the upper section 10 has an inlet port 14 for process gas and outlet ports 15 and 16 for process gas and heating gas respectively
  • the lower section has an inlet port 17 for heating gas at its lower end
  • the lower section is provided with a perforate arch member 18 above the heating gas inlet port 17 in use, the region 19 immediately above the arch 18 is filled with an inert particulate material, such as alumina spheres, to act as a flow distributor
  • a flanged ring member 20 carrying a tube assembly
  • a tube sheet 21 is welded to the lower edge of the ring member 20, and a pair of box beams 22, having a depth greater than their width, are disposed beneath the tube sheet 21 and welded thereto
  • the primary purpose of these box beams is to support the tube sheet 21 against bowing and to carry sheath tubes as described hereinafter
  • the ends of the box beams 22 also support the primary inlet headers and reactor tube assembly relative to the lower section 11 of the shell Since the weight of the assembly is borne by the ends of the box beams 22, tube sheet 21 may be of relatively light gauge construction ,
  • pairs of trunnions 23 are welded to the tube sheet 21 immediately above each box beam 22 towards the ends thereof
  • Hollow primary process gas inlet headers 24, having an elongated cross section so that their depth is substantially greater than their width, are disposed above and extend along, the box beams 22 and are mounted via supporting legs 25 and pins 26 journalled in the trunnions 23
  • the headers 24 are connected at one end by a process gas inlet conduit 27 which in turn is connected, via conduit 28, to the process gas inlet port 14 in the shell upper section 10 via bellows means (not shown) to accommodate thermal expansion
  • the tube sheet 21 , and box beams 22, may be coated with thermal insulation 29, 30 (omitted for clarity in Figures 1 and 2)
  • a plurality of secondary process gas inlet headers 31 of circular cross-section extend laterally through and are welded to the primary process gas inlet headers 24
  • This form of construction has the ancillary benefit that the portion of secondary headers 31 passing through the primary inlet headers 24 serves to strengthen the latter against the outward bowing that might result when, as is often the case, there is a significant pressure differential across the walls of the primary inlet headers 24
  • alternate secondary headers 31a are located at the lower part of the primary headers 24 while the intermediate secondary headers 31 b are located at the upper part of primary headers 24
  • Perforations, e g slots 32 or other orifices are provided through the wall of secondary inlet headers 31 to provide a flow path for process gas from the interior of primary inlet headers 24 into secondary inlet headers 31
  • Supported by brackets 33 on the primary process gas inlet headers 24 are a pair of primary process gas outlet headers 34 which are connected at one end by a process gas outlet conduit 35
  • a plurality of reactor tubes 37 extend downwards from the secondary headers 31
  • the reactor tubes 37 are disposed in sleeves 38 extending through and welded to the upper and lower sides of secondary inlet headers 31
  • Reactor tubes 37 are a sliding fit within sleeves 38 and are welded thereto at their upper ends 39 only
  • a cap 41 is welded to the top of sleeve 38
  • the reactor tube 37 can be lifted up out of sleeve 38 Since there is no weld between the lower end 40 of sleeve 38 and reactor tube 37, it is not possible to provide slots in the sleeve 38 and reactor tube 37 to provide a path for the process gas to flow from the interior of secondary header 31 into reactor tube 37 since leakage would be liable to
  • Each reactor tube 37 is of the double-tube configuration, being closed at its lower end 47 and having an inner tube 48, open at its lower end, extending down through the reactor tube 37
  • the catalyst is disposed in the annular space between the tubes 37 and 48 and is supported by a catalyst restraining grid 49 adjacent the lower end of tubes 37, 48
  • inner tube 48 is provided with an elbow 50 projecting through the wall of sleeve 38 below cap 41
  • Elbow 50 is welded to a pipe 51 connected to secondary process gas outlet headers 52 extending laterally through the primary process gas outlet headers 34
  • Perforations, e g slots, 53 are provided through that part of the wall of the secondary outlet headers 52 that is within the primary outlet headers 34 to permit flow of gas from the secondary outlet headers 52 into the primary outlet headers 34
  • tube sheet 21 are a plurality of sheath tubes 54 one for each reactor tube 37 These serve to define an annular zone outside each reactor tube 37 Since sheath tubes merely have to support their own weight and are not subject to any significant pressure differential they may be made of relatively light gauge material
  • process gas is fed through process gas inlet port 14 into the primary process gas inlet headers 24 via conduits 28 and 27, and thence, via slots 32, secondary process gas inlet headers 31 and orifice 42, conduit 45, and orifice 43 into the annular space in the reactor tubes 37 between the interior wall thereof and the associated inner tube 48
  • the process gas undergoes the desired reaction and then passes up inner tube 48 and into process gas outlet headers 52 via pipe 51 , the secondary process gas outlet header 52 and slots 53
  • the process gas then leaves the vessel via conduits 35 and 36 and process gas outlet port 15
  • the heating gas is fed to the vessel via inlet port 17, and after flow through perforate arch 18 and the packing in the flow distributor region 19, flows up the annulus between each sheath tube 54 and its associated reforming tube 37, into the space above tube sheet 21 From there it leaves the vessel via heating gas outlet port 16
  • the caps 41 can be removed by removing the welds at the top of sleeves 38 If it is necessary
  • the primary inlet header 24 is supported directly on a flange 55 provided on the inner wall of the flanged ring member 20 which in turn is supported on a flange 56 on the lower portion 1 1 of the shell
  • the shell is shown with an external cooling jacket 57 through which a suitable coolant medium, for example boiling water, is circulated This ensures that the shell is maintained at a temperature not much above 100°C, even though the heating gas inside the shell may be at a temperature of for example 900°C or more
  • a suitable coolant medium for example boiling water
  • sheath tubes 54 and the primary inlet headers 24 inevitably are at a relatively high temperature and necessarily have metal-to-metal contact with the flanged ring member 20 By providing a sufficient depth to the flanged ring member, the thermal gradient therein can be maintained at an acceptable level

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • General Health & Medical Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne un réacteur à échange thermique comportant une enveloppe extérieure (10) pourvue d'un orifice d'admission des gaz (14) et des orifices de sortie (15, 16), une pluralité de tubes de réacteur (54) supportés par leurs extrémités supérieures, un dispositif collecteur (24) comprenant au moins deux collecteurs d'admission primaires (24) disposés sur la partie supérieure de ladite enveloppe (10), chaque collecteur d'admission primaire (24) ayant une profondeur supérieure à sa largeur, lesdits tubes (54) étant supportés, par rapport à l'enveloppe (10), directement ou indirectement par lesdits collecteurs d'admission primaires (24).
EP01900171A 2000-02-01 2001-01-04 Reacteur a echange thermique Withdrawn EP1251952A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
GB0002153 2000-02-01
GBGB0002153.5A GB0002153D0 (en) 2000-02-01 2000-02-01 Heat exchange reactor
PCT/GB2001/000026 WO2001056690A1 (fr) 2000-02-01 2001-01-04 Reacteur a echange thermique

Publications (1)

Publication Number Publication Date
EP1251952A1 true EP1251952A1 (fr) 2002-10-30

Family

ID=9884648

Family Applications (1)

Application Number Title Priority Date Filing Date
EP01900171A Withdrawn EP1251952A1 (fr) 2000-02-01 2001-01-04 Reacteur a echange thermique

Country Status (6)

Country Link
EP (1) EP1251952A1 (fr)
JP (1) JP2003521371A (fr)
KR (1) KR20030004336A (fr)
AU (1) AU2001223848A1 (fr)
GB (1) GB0002153D0 (fr)
WO (1) WO2001056690A1 (fr)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100838970B1 (ko) 2005-04-29 2008-06-16 주식회사 엘지화학 유량 배분 균일성이 향상된 환상도관
BRPI0813997B1 (pt) * 2007-07-05 2017-07-04 Saudi Basic Industries Corporation Reactor panel for catalytic processes
FR2918904B1 (fr) 2007-07-20 2011-07-15 Inst Francais Du Petrole Reacteur echangeur a tube baionnette permettant de fonctionner avec des differences de pression de l'ordre de 100 bars entre le cote tube et le cote calandre.
KR101109154B1 (ko) * 2009-03-13 2012-02-16 서강대학교산학협력단 반응기
WO2013004254A1 (fr) 2011-07-01 2013-01-10 Haldor Topsøe A/S Réacteur échangeur de chaleur
FR2979257B1 (fr) 2011-08-26 2013-08-16 Ifp Energies Now Reacteur echangeur pour la production d'hydrogene avec faisceau de generation vapeur integre
US11260357B2 (en) 2017-12-21 2022-03-01 Uop Llc Process and apparatus for fluidizing a catalyst bed
US20240293787A1 (en) 2021-01-28 2024-09-05 Topsoe A/S Catalytic heat exchange reactor with helical flow

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3119671A (en) * 1960-09-28 1964-01-28 Chemical Coustruction Corp Upright fluid heating furnace with heat recovery system
DE1235494B (de) * 1963-04-10 1967-03-02 Power Gas Ltd Reformiervorrichtung mit an den unteren Enden geschlossenen Reformierrohren

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO0156690A1 *

Also Published As

Publication number Publication date
JP2003521371A (ja) 2003-07-15
KR20030004336A (ko) 2003-01-14
AU2001223848A1 (en) 2001-08-14
WO2001056690A1 (fr) 2001-08-09
GB0002153D0 (en) 2000-03-22

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