New! View global litigation for patent families

DE4313723A1 - Reactor with oxidation catalyst - Google Patents

Reactor with oxidation catalyst

Info

Publication number
DE4313723A1
DE4313723A1 DE19934313723 DE4313723A DE4313723A1 DE 4313723 A1 DE4313723 A1 DE 4313723A1 DE 19934313723 DE19934313723 DE 19934313723 DE 4313723 A DE4313723 A DE 4313723A DE 4313723 A1 DE4313723 A1 DE 4313723A1
Authority
DE
Grant status
Application
Patent type
Prior art keywords
frames
reactor
catalyst
another
invention
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Withdrawn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
DE19934313723
Other languages
German (de)
Inventor
Wolfgang Fahrnschon
Peter Kripylo
Juergen Koppe
Walter Leipnitz
Original Assignee
Koppe Juergen Dr
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

Links

Classifications

    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00Catalysts, in general, characterised by their form or physical properties
    • B01J35/02Solids
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/16Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/20Vanadium, niobium or tantalum
    • B01J23/22Vanadium
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical 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
    • B01J8/0285Heating or cooling the reactor
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical 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
    • B01J8/04Chemical 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 the fluid passing successively through two or more beds
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02Chemical 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
    • B01J8/04Chemical 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 the fluid passing successively through two or more beds
    • B01J8/0496Heating or cooling the reactor
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/78Preparation by contact processes characterised by the catalyst used
    • C01B17/79Preparation by contact processes characterised by the catalyst used containing vanadium
    • CCHEMISTRY; METALLURGY
    • C01INORGANIC CHEMISTRY
    • C01BNON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B17/00Sulfur; Compounds thereof
    • C01B17/69Sulfur trioxide; Sulfuric acid
    • C01B17/74Preparation
    • C01B17/76Preparation by contact processes
    • C01B17/80Apparatus
    • C01B17/803Converters
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008Controlling the process
    • B01J2208/00017Controlling the temperature
    • B01J2208/00106Controlling the temperature by indirect heat exchange
    • B01J2208/00168Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00194Tubes
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796Details of the reactor or of the particulate material
    • B01J2208/00805Details of the particulate material
    • B01J2208/00814Details of the particulate material the particulate material being provides in prefilled containers
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS, COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/18Details relating to the spatial orientation of the reactor
    • B01J2219/182Details relating to the spatial orientation of the reactor horizontal

Abstract

The invention relates to a reactor having an oxidation catalyst incorporated in the mechanical structure and three-dimensionally integrated heat exchangers for preparing sulphur trioxide from sulphur dioxide and air and simultaneously generating high-pressure steam. This object is achieved according to the invention by vertically positioned frames being arranged next to one another as sections, with frames in which the metal sponge having the active catalytic composition located on the surface is inserted in a vertical position being followed by frames containing the known tube boiler elements as steam generators, and the individual frames being firmly but detachably connected with one another to give a sandwich reactor.

Description

Die Erfindung betrifft einen Reaktor mit in dem mechanischen Aufbau einbezogenen Oxidationskatalysator und räumlich inte grierten Wärmetauschern zur Herstellung von Schwefeltrioxid aus Schwefeldioxid und Luft und gleichzeitiger Erzeugung von Hochdruckwasserdampf. The invention relates to a reactor included in the mechanical structure of the oxidation catalyst and spatially inte grated heat exchangers for the production of sulfur trioxide from sulfur dioxide and air, and simultaneous generation of high pressure steam.

Nach dem Stand der Technik werden heute ausnahmslos Oxida tionskatalysatoren verwendet, die aus der aktiven katalyti schen Masse, vermischt mit unterschiedlichen keramischen Trä germaterialien bestehen und zu Kugeln, Strangabschnitten, Ringen oder Sternen verformt worden sind. According to the prior art are without exception now tion catalysts Oxida used, the mixed mass from the active rule katalyti with different ceramic Trä consist germaterialien and have been formed into spheres, extruded sections, rings or stars. Diese Katalysatoren lassen sich nur in Schüttungen verwenden, vorzugsweise in waagerechten Horden, die in übereinander angeordneten Etagen nacheinander durchströmt werden. These catalysts can only be used in beds, preferably in horizontal trays, which are flowed through in superposed floors sequentially. Die bei der Oxidation frei werdende Wärme muß durch Wärmeaustauscher abgeführt werden. The energy released by the oxidation heat must be dissipated through heat exchangers. Dazu wird der Gasstrom mehrmals aus dem Reaktor heraus und nach dem Wärmetausch wieder hineingeführt. For this purpose, the gas stream is guided several times out of the reactor and after the heat exchange again. Reaktor und Wärme tauscher bilden kein einheitliches Bauwerk (deutsche Patent schrift Nr. 28 38 112). Reactor and heat exchanger is no single building form (German Pat. No. 28 38 112). Es wurde auch versucht, Reaktoren mit senkrechten gasdurchlässigen Wänden zu bauen, die eine waa gerechte Durchströmung der Katalysatorschüttung ermöglichen sollten, (deutsche Patentschrift Nr. 37 40 255). It was also tried to build reactors with vertical gas-permeable walls, which should allow a waa just flow through the catalyst bed, (German Pat. No. 37 40 255). Auch die Ver wendung eines monolytischen Kontaktes mit 775 Kanälen auf einen Quadratdezimeter wird vorgeschlagen (deutsche Patent schrift Nr. 31 28 060). Also, the use of a monolithic Ver contact with 775 channels on a square decimeter is proposed (German Pat. No. 31 28 060). Mit einem Konvertierungssystem, das aus einer beliebigen Anzahl gesonderter Kontaktöfen besteht, von welchen jeder eine Katalysatorschicht und einen Wärmetauscher in einem gemeinsamen Gehäuse enthält, wird versucht, den Rohr leitungsbedarf zu minimieren (deutsche Patentschrift Nr. 29 21 024). With a conversion system that consists of any number of separate Kontaktöfen, each of which contains a catalyst layer and a heat exchanger in a common housing, it is attempted to minimize the piping required (German Pat. No. 29 21 024). Auch große Röhrenreaktoren mit einer Vielzahl von Rohren mit innen befindlicher Katalysatorschüttung und Flüs sigkeitskühlung von außen, sind als Lösung aufgezeigt worden deutsche Patentschrift Nr. 30 06 900). Also large tubular reactors having a plurality of tubes with internal befindlicher catalyst bed and flues sigkeitskühlung from the outside, have been demonstrated as a solution German Pat. No. 30 06 900).

Allen vorgeschlagenen und praktizierten Lösungen haftet der Mangel an, daß der Katalysator mit einem die Wärme nur wenig leitenden keramischen Träger verbunden ist, der zudem noch keine allzugroße mechanische Festigkeit besitzt und nicht abriebfest ist. All proposed and practiced solutions adhered to the defect that the catalyst is connected to a heat only slightly conductive ceramic support, which also still has no great mechanical strength and is not resistant to abrasion. Die Folge ist, daß ein großer Volumenanteil des Katalysators wegen innerer Überhitzung unwirksam ist, daß der Reaktor um die Katalysatorschüttung herum gebaut werden muß und daß, um allzu große Bauhöhen zu vermeiden, die notwen digen Wärmetauscher außerhalb des Reaktors stehen müssen, was lange Gaswege zwischen den einzelnen Aggregaten erfordert. that a large volume fraction of the catalyst is ineffective due to internal overheating that the reactor to the catalyst bed around has to be built and that in order to avoid excessive heights, must be the notwen ended heat exchanger outside the reactor, which long gas lines is the result between requires the individual units. Auch die Gasverteilung muß vor jeder Katalysatorschicht nach dem Wärmetausch neu vorgenommen werden, was zusätzlichen Raum im Reaktor erfordert. The gas distribution must be made again before each catalyst layer after heat exchange, which requires additional space in the reactor.

Das Ziel der Erfindung ist es, die die bekannten Oxidations katalysatoren beeinträchtigenden Nachteile, wie geringe Wärme leitfähigkeit, keine Möglichkeit der konstruktivtragenden Integration des Katalysatorträgers in das Reaktorbauwerk, bis herige räumliche Trennung von Reaktor und Wärmetauscher zu beseitigen. The aim of the invention is the conductivity of the known oxidation catalysts debilitating drawbacks such as low heat, no possibility of konstruktivtragenden integration of the catalyst carrier in the reactor building up THE PREVIOUS spatial separation of reactor and heat exchanger to be eliminated.

Der Erfindung liegt die Aufgabe zugrunde, einen neuartigen Reaktor zu entwickeln, der als ein Bauelement Metallschwamm mit aufgebrachter, katalytisch wirksamer aktiver Masse als Oxidationskatalysator enthält und dadurch die gekoppelte Her stellung von Schwefeltrioxid und Hochdruckdampf in einem Bau körper ermöglicht. The invention has for its object to develop a new reactor, which contains, as a component metal sponge with applied catalytically active material effective as an oxidation catalyst and in the coupled position of Her sulfur trioxide and high-pressure steam in a construction body made possible.

Die Aufgabe wird erfindungsgemäß gelöst, indem senkrecht ste hende Rahmen als Sektionen nebeneinander angeordnet sind, wobei Rahmen, in die Metallschwamm mit der auf der Oberfläche befindlichen aktiven katalytischen Masse senkrecht stehend eingefügt ist, von Rahmen gefolgt werden, die bekannte Rohr kesselelemente als Dampferzeuger enthalten und die einzelnen Rahmen fest, aber lösbar miteinander zu einem Sandwichreaktor verbunden sind. The object is achieved according to the invention, by vertically ste rising frames are arranged as sections next to each other, wherein the framework is inserted upright in the metal sponge with the present on the surface active catalytic mass, followed by frame, the known tube boiler elements included as a steam generator and the individual frames firmly, but detachably connected to each other to form a sandwich reactor.

Die Erfindung soll anhand des folgenden Beispiels erläutert werden. The invention will be illustrated by the following example.

Beispiel example

Wie aus den Abb. 1 (Draufsicht) und 2 (Seitenansicht) zu entnehmen ist, sind die Rahmen, in denen der Katalysator angeordnet ist, so gestaltet, daß das Metallschwammgefüge etwa 0,5 m dick ist. As seen from Fig. 1 (plan view) and 2 (side view) it can be seen, the frame in which the catalyst is arranged, designed so that the metal sponge structure is about 0.5 m thick.

Bei der Rahmengröße 5,5 × 12 m (5,5 m Höhe, 12 m Breite) können in einem Rahmen etwa 33 Kubikmeter Katalysatorschwamm untergebracht werden. When the frame size 5.5 × 12 m (5.5 m in height, 12 m width) can be accommodated in one frame is approximately 33 cubic meters of catalyst sponge. In fünf Rahmen sind somit insgesamt 165 Kubikmeter Katalysatorschwamm enthalten. In five frames thus contained a total of 165 cubic meters of catalyst sponge. Die Rahmen sind als senkrechtes Gitterwerk aufgebaut, in das die Katalysator schwammpakete eingefügt sind. The frames are constructed as a vertical lattice, in which the catalyst is inserted sponge packages.

Nach der ersten Sektion (Rahmen) Katalysator K1 sind in Strö mungsrichtung die Sektionen W1 bis W3 angeordnet, von denen W1 ein Dampfüberhitzer, W2 und W3 je eine Verdampfersektion sind, da in der ersten Sektion Katalysator K1 etwa 60% des Schwefeltrioxids und der Wärme entstehen. After the first section (frames) catalyst K1 are in Strö flow direction, the sections W1 arranged to W3, of which W1, a steam superheater, W2 and W3 each an evaporator section, since about 60% of the sulfur trioxide and the heat generated in the first section of catalyst C1 , Dann folgen die zweite Sektion Katalysator K2, die Sektion Verdampfer W4, die Sektion Katalysator K3, die Sektion Verdampfer W5. Followed by the second section of catalyst K2, the evaporator section W4, the K3 catalyst section, the section evaporator W5. Für den Fall, daß nach dem Doppelkatalyseverfahren gearbeitet wird, folgt jetzt der Gassammler G1, durch den das Reaktions gemisch aus dem Reaktor herausgeführt wird. In the event that it is carried by the double catalysis method now follows the gas collector G1, by which the reaction mixture is led out of the reactor.

Über den Gasverteiler V2 erfolgt die Wiedereinführung in den Reaktor. Via the gas distributor V2 the reintroduction takes place in the reactor. Nach dem Durchströmen der Sektionen K4 und K5 folgt die Sektion Wassererhitzer W6, in der das Kesselspeisewasser auf die Verdampfertemperatur gebracht wird. After flowing through the sections K4 and K5, the water heater section W6 in which the boiler feed water is brought to the evaporator temperature follows. Der sich anschlie ßende Gassammler G2 dient zum Herausführen des nunmehr voll ständig umgesetzten Reaktionsgemisches aus dem Reaktor. Which subsequently sequent gas collector G2 is used for feeding out the now fully continuously converted reaction mixture from the reactor.

Der Reaktor mit integriertem Dampferzeuger hat eine Gesamt länge von etwa 15 m und leistet in 24 Stunden 800 t Schwefel trioxid, 336 t Hochdruckdampf (450 Grad Celsius, 41 bar) und zusätzlich 340 t Heißwasser (260 Grad Celsius, 41 bar). The reactor with integrated steam generator has an overall trioxide length of about 15 m and provides within 24 hours 800 tons of sulfur, 336 t high-pressure steam (450 degrees Celsius, 41 bar) and in addition 340 t hot water (260 degrees Celsius, 41 bar).

Bezugszeichenliste LIST OF REFERENCE NUMBERS

K1 Katalysator Sektion 1 K1 catalyst section 1
K2 Katalysator Sektion 2 K2 catalyst Section 2
K3 Katalysator Sektion 3 K3 catalyst Section 3
K4 Katalysator Sektion 4 K4 catalyst section 4
K5 Katalysator Sektion 5 K5 catalyst section 5
W1 Wärmetauscher Sektion 1 Überhitzer W1 heat exchanger section 1 superheater
W2 Wärmetauscher Sektion 2 Verdampfer W2 heat exchanger section 2 evaporator
W3 Wärmetauscher Sektion 3 Verdampfer W3 heat exchanger section 3 Evaporator
W4 Wärmetauscher Sektion 4 Verdampfer W4 heat exchanger section 4 Evaporator
W5 Wärmetauscher Sektion 5 Verdampfer W5 heat exchanger section 5 Evaporator
W6 Wärmetauscher Sektion 6 Wassererhitzer W6 heat exchanger section 6 water heater
V1 Gasverteiler Sektion 1 V1 Gas distribution Section 1
V2 Gasverteiler Sektion 2 V2 gas distribution section 2
G1 Gassammler Sektion 1 G1 gas collector section 1
G2 Gassammler Sektion 2 G2 gas collector section 2
E1 Reaktionsgemisch Eingang E1 reaction mixture input
E2 Kesselspeisewasser Eingang E2 boiler feed water input
A1 Reaktionsgemisch Ausgang A1 reaction mixture output
A2 Hochdruckdampf Ausgang A2 high-pressure steam output
Z1 Reaktionsgemisch zur Zwischenabsorption Z1 reaction mixture for the intermediate absorption
Z2 Reaktionsgemisch von der Zwischenabsorption Z2 reaction mixture of the intermediate absorption

Claims (3)

1. Reaktor mit Oxidationskatalysator, der bekannte Rohrkessel elemente als Wärmetauscher in Strömungsrichtung des Reaktions gemisches enthält, dadurch gekennzeichnet, daß senkrecht ste hende Rahmen als Sektionen nebeneinander angeordnet sind, wobei nach jeweils ein oder zwei Sektionen mit Katalysator K1 bis K5 in den Abb. 1 und 2) ein oder mehrere Sektionen, die bekannte Rohrkesselelemente als Wärmetauscher enthalten, (W1 bis W6 in den Abb. 1 und 2) in Strö mungsrichtung des Reaktionsgemisches folgen und diese Sektio nen, von denen jede aus einem Rahmen mit darin angeordnetem senkrechten Gitterwerk besteht, lösbar direkt miteinander verbunden sind, wobei in den Sektionen K1 bis K5 im Gitter werk senkrecht stehend die Pakete des Katalysators, der aus einem offenzelligen, großporigen Metallschwamm mit einer Po rengröße von 0,1 bis 10,0 mm Durchmesser, auf dessen Ober fläche die katalytisch wirksame Masse Vanadiumpentoxid und Zusatzkomponenten aufgebracht ist, besteht, eingefü 1st reactor with the oxidation catalyst, the known tube boiler elements as a heat exchanger in the flow direction of the reaction mixture contains, characterized in that perpendicular ste rising frames are arranged as sections next to each other, wherein after one or two sections with catalyst K1 to K5 in the Fig. 1 and 2) one or more sections which contain known tube boiler elements as a heat exchanger (W1 to W6 in Fig. 1 and 2) in Strö flow direction to follow and NEN this Caesarean section, each of which consists of a frame having arranged therein vertical latticework of the reaction mixture are detachably connected directly to each other, wherein in the sections K1 to K5 in the lattice standing vertically, the packets of the catalyst rengröße of an open cell, large-pored metal sponge having a Po of 0.1 to 10.0 mm in diameter, on its upper surface the catalytically active composition comprises vanadium pentoxide and additional components is applied, there is, eingefü gt sind und die Sektionen V1 und V2 in den Abb. 1 und 2, die Verteiler für das in den Reaktor eintretende, die Sektionen G1 und G2 in den Abb. 1 und 2 die Sammler für das aus dem Reaktor herauszuführende Reaktionsgemisch sind, wobei sich zwischen den Sektionen G1 und V2 eine gasundurchlässige Trennwand befindet. are gt and sections V1 and V2 in the Fig. 1 and 2, the distribution for entering the reactor, the sections G1 and G2, the collector are shown in Figs. 1 and 2 for the herauszuführende from the reactor the reaction mixture, wherein G1 and V2 is a gas impermeable partition wall between the sections.
2. Reaktor mit Oxidationskatalysator gemäß Anspruch 1 dadurch gekennzeichnet, daß auf den Gassammler G1 und den Gasvertei ler V2 verzichtet wird. 2nd reactor with the oxidation catalyst according to claim 1 characterized in that ler is omitted V2 on the gas collector G1 and Gasvertei.
3. Reaktor mit Oxidationskatalysator gemäß Anspruch 1 und 2 da durch gekennzeichnet, daß an Stelle des Metallschwammkatalysa tors ein konventioneller Katalysator eingesetzt wird. 3. reactor with the oxidation catalyst according to claim 1 and 2 as that in place of the gate Metallschwammkatalysa a conventional catalyst is used characterized by.
DE19934313723 1993-04-27 1993-04-27 Reactor with oxidation catalyst Withdrawn DE4313723A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
DE19934313723 DE4313723A1 (en) 1993-04-27 1993-04-27 Reactor with oxidation catalyst

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DE19934313723 DE4313723A1 (en) 1993-04-27 1993-04-27 Reactor with oxidation catalyst

Publications (1)

Publication Number Publication Date
DE4313723A1 true true DE4313723A1 (en) 1994-11-03

Family

ID=6486474

Family Applications (1)

Application Number Title Priority Date Filing Date
DE19934313723 Withdrawn DE4313723A1 (en) 1993-04-27 1993-04-27 Reactor with oxidation catalyst

Country Status (1)

Country Link
DE (1) DE4313723A1 (en)

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001054806A1 (en) * 2000-01-25 2001-08-02 Meggitt (Uk) Ltd Chemical reactor with heat exchanger
US7033553B2 (en) 2000-01-25 2006-04-25 Meggitt (Uk) Limited Chemical reactor
US7967878B2 (en) 2002-01-04 2011-06-28 Meggitt (Uk) Limited Reformer apparatus and method
US8177868B2 (en) 2002-01-04 2012-05-15 Meggitt (Uk) Limited Reforming apparatus and method

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001054806A1 (en) * 2000-01-25 2001-08-02 Meggitt (Uk) Ltd Chemical reactor with heat exchanger
US7033553B2 (en) 2000-01-25 2006-04-25 Meggitt (Uk) Limited Chemical reactor
US7967878B2 (en) 2002-01-04 2011-06-28 Meggitt (Uk) Limited Reformer apparatus and method
US8177868B2 (en) 2002-01-04 2012-05-15 Meggitt (Uk) Limited Reforming apparatus and method
US8758459B2 (en) 2002-01-04 2014-06-24 Meggitt (Uk) Limited Reforming apparatus and method
US8882865B2 (en) 2002-01-04 2014-11-11 Meggitt (Uk) Ltd. Reformer apparatus and method with heat exchange occurring through a cross-flow configuration
US9617152B2 (en) 2002-01-04 2017-04-11 Meggitt (Uk) Limited Reforming apparatus and method

Similar Documents

Publication Publication Date Title
US5635145A (en) Multi-bed downflow reactor
EP0977294B1 (en) High temperature fuel cells installation
DE19544895C1 (en) Oxidising carbon mon:oxide in gas mixt. from hydrocarbon reforming plant
EP0700714A1 (en) Process for the catalytic vapour phase oxidation of propylene to acrolein
EP0285845A1 (en) Method and device for pressure suppression of a nuclear power plant
DE3708957A1 (en) Reactor for the catalytic conversion of H2S and SO2 present in a gas stream into elemental sulphur
DE19720205A1 (en) Purification of exhaust gases charged with nitrogen oxide(s)
DE3916325A1 (en) Moving bed reactor system
EP0885653A2 (en) Compact fixed bed reactor for catalytic reactions with integral heat exchange
US3642452A (en) Multistage reactors
EP0330751A2 (en) Process for producing a synthesis gas containing hydrogen and carbon monoxide, and apparatus therefor
EP0036142B1 (en) Bundle of fuel elements
EP0384200A1 (en) Steam condenser
DE102004017150A1 (en) Partial oxidation in gas phase of three and/or four carbon precursor compounds to (meth)acrolein and/or (meth)acrylic acid with particulate catalyst in reactor having cuboidal thermoplate modules, cylindrical shell, and sealing element(s)
EP0534195A1 (en) Reactor and process for carrying out heterogeneous catalytic reactions
US2418673A (en) Method for catalytic conversion of hydrocarbons
US5919405A (en) Fluid distribution system for an absorption tower
EP0326667A1 (en) Catalyst for selective reduction of nitrogen oxides
DE4305001A1 (en) Apparatus for oxychlorination
DE102008040544A1 (en) Reaction vessel and method for using
EP0945174A1 (en) Reactor unit for a catalytic chemical reaction, specifically for catalytic reforming of methanol
US2436780A (en) Method for handling a contact mass
EP0444732A1 (en) Fluidized bed reactor
DE19806810A1 (en) Catalytic tube reactor useful for production of maleic and phthalic acid anhydrides, acrolein and acrylic acid
DE3629894A1 (en) Plant for surface finishing by of continuously moving bands, particularly pickling plant

Legal Events

Date Code Title Description
8122 Nonbinding interest in granting licenses declared
8139 Disposal/non-payment of the annual fee