DE1142586B - Process and device for gas supply in catalytic high pressure reactors - Google Patents

Process and device for gas supply in catalytic high pressure reactors

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Publication number
DE1142586B
DE1142586B DEL37594A DELO027594A DE1142586B DE 1142586 B DE1142586 B DE 1142586B DE L37594 A DEL37594 A DE L37594A DE LO027594 A DELO027594 A DE LO027594A DE 1142586 B DE1142586 B DE 1142586B
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Prior art keywords
gas
catalyst
heat exchanger
main heat
containers
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DEL37594A
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German (de)
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Dr Helmut Hinrichs
Dipl-Ing Johann Niedetzky
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Lentia GmbH
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Lentia GmbH
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Publication of DE1142586B publication Critical patent/DE1142586B/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • C01C1/0435—Horizontal reactors
    • 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
    • B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
    • B01J3/04—Pressure vessels, e.g. autoclaves
    • 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
    • B01J8/0005—Catalytic processes under superatmospheric pressure
    • 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
    • B01J8/04—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 the fluid passing successively through two or more beds
    • B01J8/0403—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 the fluid passing successively through two or more beds the fluid flow within the beds being predominantly horizontal
    • 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
    • B01J8/04—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 the fluid passing successively through two or more beds
    • B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • 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
    • B01J8/04—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 the fluid passing successively through two or more beds
    • B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0461—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
    • B01J8/0469—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being superimposed one above the other
    • 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
    • B01J8/04—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 the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • 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
    • B01J2208/00194—Tubes
    • 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
    • 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
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Description

Verfahren und Vorrichtung zur Gasführung in katalytischen Hochdruckreaktoren Für exotherm verlaufende katalytische Hochdrucksynthesen zur Herstellung von Ammoniak, aber auch von Methanol u. a. besteht die Forderung, die Reaktion vom Anfang bis zum Ende bei der optimalen Reaktionstemperatur ablaufen zu lassen. Hiedurch bedingt sind zahlreiche Verfahren bekanntgeworden, durch Aufwärmung des Eingangsgasgemisches bzw. Abkühlung des ausreagierten Gases der Einhaltung einer idealen Temperaturkurve der Reaktion nahezukommen. Es sei hier nur auf die unterschiedlichen Versuche zur optimalen Verteilung bzw. Abführung des Wärmeüberschusses der exothermen Reaktion verwiesen, bei denen Kontaktröhren- und Kühlröhrensysteme mit parallel oder in Serie angeordneten Vollraumschüttungen abwechseln, sowie auf besondere Kühleinrichtungen durch reaktionsfremde Kühlmittel, etwa in Form von Wasserrohrschlangen zwischen einzelnen Kontaktlagen oder als indirekte und direkte Kaltgaszuführungen zur oder nach der heißesten Reaktionszone.Method and device for conducting gas in catalytic high-pressure reactors For exothermic catalytic high pressure syntheses for the production of ammonia, but also of methanol and others. there is a requirement to have the response from the beginning up to run to the end at the optimal reaction temperature. Due to this Numerous processes have become known by heating the input gas mixture or cooling of the reacted gas in compliance with an ideal temperature curve get close to the reaction. Let us just refer to the different experiments optimal distribution or removal of the excess heat of the exothermic reaction referenced in which contact tube and cooling tube systems with parallel or in series arranged full-volume fillings, as well as on special cooling devices by non-reactive coolants, for example in the form of water coils between individual contact layers or as indirect and direct cold gas feeds to or after the hottest reaction zone.

Diese Einrichtungen waren einerseits kompliziert, andererseits wurde der Gehalt des ausreagierten Gases an Syntheseendprodukt durch Frischgaszuführung oft stark verdünnt. Die Druckwasserkühlung durch Rohrschlangen sowie die Öfen mit ausschließlicher Kaltgaszuführung zwischen die einzelnen Kontaktlagen bedingen wieder einen Hauptwärmeaustauscher mit sehr langen Rohren, um das Frischgas doch noch mit der nötigen Eingangstemperatur auf den Katalysator zu bringen.These facilities were on the one hand complicated, on the other hand it was the content of the reacted gas in the synthesis end product from the supply of fresh gas often very diluted. The pressurized water cooling through pipe coils as well as the ovens with exclusive cold gas supply between the individual contact layers require again a main heat exchanger with very long pipes to still have the fresh gas to bring the necessary inlet temperature to the catalyst.

Gemäß der nachfolgend beschriebenen Erfindung wird bei einem Hochdruckreaktor, der innerhalb eines in einem Druckmantel befindlichen Einsatzmantels zwei oder mehrere in Serie geschaltete Katalysatorbehälter und einen endständigen Hauptwärmetauscher enthält, das gesamte Frischgasgemisch in bestimmter Weise zur Gegenstromkühlung des durch die exotherme Reaktion aufgeheizten Synthesegases herangezogen, bevor es auf die erste Kontaktlage aufgegeben wird.According to the invention described below, in a high pressure reactor, the two or more within an insert jacket located in a pressure jacket catalytic converter tanks connected in series and a terminal main heat exchanger contains, the entire fresh gas mixture in a certain way for countercurrent cooling of the synthesis gas heated by the exothermic reaction is used before it is given up on the first contact position.

Das erfindungsgemäße Verfahren zur Gasführung in katalytischen Hochdrucksyntheseanlagen mit zwei oder mehreren in einem Einsatzmantel übereinander angeordneten, im Gaswege miteinander verbundenen Katalysatorbehältern ist dadurch gekennzeichnet, daß das an einem Ende des Ofens aufgegebene kalte Eingangsgasgemisch einen durch den Druckmantel (1, 2,3) und den die Katalysatorbehälter umschließenden Einsatzmantel (4) gebildeten, an sich bekannten peripheren Ringraum (5) und sodann einen am entgegengesetzten Ende des Ofens befindlichen, ebenfalls an sich bekannten Hauptwärmeaustauscher (6) durchströmt, wonach es, teilweise aufgewärmt, innerhalb des Einsatzmantels (4) im Gegenstrom zum Eingangsgasstrom entweder nacheinander die Außenseite der Wände der einzelnen Katalysatorbehälter (7 bis 10) umströmt oder diese letzteren durch zentral angeordnete Gasdurchlässe (12) nacheinander durchströmt, wobei zwischen den einzelnen Katalysatorbehältern angeordnete und diese miteinander verbindende kurze Austauscherrohre (11) gekühlt werden, und das Gas anschließend auf die oberste Katalysatorlage (7) aufgegeben und in neuerlicher Umkehr der Strömungsrichtung die einzelnen Katalysatorbehälter (7 bis 10) und die Austauscherrohre (11) durchströmt und den Ofen durch den Hauptwärmeaustauscher (6) hindurch verläßt.The method according to the invention for conducting gas in catalytic high-pressure synthesis plants with two or more catalyst containers arranged one above the other in an insert jacket and interconnected in the gas path is characterized in that the cold input gas mixture fed into one end of the furnace is passed through the pressure jacket (1, 2, 3) and the the insert jacket (4) which surrounds the catalyst container and which is known per se and then flows through a main heat exchanger (6) located at the opposite end of the furnace, also known per se, after which it is partially warmed up inside the insert jacket (4) Countercurrent to the inlet gas flow either flows around the outside of the walls of the individual catalyst containers (7 to 10 ) one after the other or flows through the latter one after the other through centrally arranged gas passages (12) , with short ones arranged between the individual catalyst containers and connecting them to one another Exchanger tubes (11) are cooled, and the gas is then applied to the topmost catalyst layer (7) and, in a renewed reversal of the direction of flow, flows through the individual catalyst containers (7 to 10) and the exchanger tubes (11) and through the furnace through the main heat exchanger (6) leaves.

Durch die an sich bekannte Unterteilung der Kontaktmasse in einzelne Lagen und durch den jeweils fortschreitenden Wärmetausch zwischen diesen Kontaktlagen gemäß den Anweisungen der Erfindung sowie durch die erfindungsgemäße Heranziehung ausschließlich von Frischgas zur Gegenstromkühlung aller Katalysatorlagen des Reaktors wird einerseits jede Verdünnung des zur Umsetzung gebrachten Synthesegases mit allen ihren Nachteilen vermieden und andererseits ein optimaler Temperaturkurvenverlauf erzielt, der bei höchster Wirtschaftlichkeit optimalen Aufbau des Syntheseproduktes sichert. Vor allem aber wird durch die erfindungsgemäße Führung des gesamten Frischgases erreicht, daß das Frischgas nicht schon in dem bisher bekannten Hauptwärmetauscher auf die Anspringtemperatur des Katalysators aufgewärmt werden muß, sondern daß diese Aufwärmung in den nachfolgenden kurzen Austauscherrohren zwischen den einzelnen Kontaktlagen erfolgt.By dividing the contact mass into individual ones, which is known per se Layers and due to the progressive heat exchange between these contact layers according to the instructions of the invention as well as by the use of the invention exclusively of fresh gas for countercurrent cooling of all catalyst zones of the reactor on the one hand, every dilution of the synthesis gas brought into reaction with all of them their disadvantages avoided and on the other hand an optimal temperature curve achieved, the optimum with the highest economic efficiency construction of Synthetic product secures. But above all, the inventive leadership of the entire fresh gas achieved that the fresh gas is not already in the previously known Main heat exchanger to be warmed up to the light-off temperature of the catalyst must, but that this warming up in the subsequent short exchanger tubes takes place between the individual contact layers.

Es ist bereits bekannt, das Frischgas nach dem Passieren eines Hauptwärmeaustauschers in einem Ringraum an der Außenwand eines oder mehrerer hintereinandergeschalteter Katalysatorbehälter entlangzuführen (deutsche Patentschrift 1009 602). Dieses an sich bekannte Einzelmerkmal erlangt im beanspruchten Verfahren nur in Verbindung mit den übrigen erfindungsgemäßen Merkmalen Bedeutung.It is already known that the fresh gas after passing through a main heat exchanger one or more series-connected in an annular space on the outer wall Guide along the catalyst container (German patent specification 1009 602). This on known individual feature is only obtained in connection in the claimed method with the other features according to the invention meaning.

Durch Regelung der Höhe der einzelnen Katalysatorlagen bzw. der Länge der Austauscherrohre gelingt es, die Einhaltung eines praktisch idealen Temperaturverlaufes über die Gesamtschicht des Katalysators zu sichern. Außerdem wird der endständige Hauptwärmeaustauscher weitgehend entlastet, wodurch er beträchtlich kleiner gehalten werden kann, was wiederum einer besseren Ausnutzung des Druckkörpervolumens durch Vermehrung der Katalysatormenge und damit einer Erhöhung der Ofenleistung gleichkommt.By regulating the height of the individual catalyst layers or the length the exchanger tubes succeed in maintaining a practically ideal temperature profile secure over the entire layer of the catalyst. In addition, the terminal Main heat exchanger largely relieved, which means it is kept considerably smaller can be, which in turn enables better utilization of the pressure hull volume Increasing the amount of catalyst and thus an increase in the furnace output is equivalent.

Diese Wirkung kann erfindungsgemäß noch dadurch verstärkt werden, daß das aufsteigende Frischgas nicht, wie zuvor geschildert, die einzelnen Katalysatorbehälter umspült, sondern diese letzteren durch zentral angeordnete Durchlaßöffnungen durchströmt. Hierbei kann auch noch auf den peripheren Ringraum zwischen dem Einsatzmantel und den Katalysatorbehältern verzichtet werden, wodurch weiterer Katalysatorraum gewonnen werden kann und die Möglichkeit gegeben ist, die Katalysatorbehälter unter Entlastung der Austauscherrohre zwischen diesen bzw. unter Entlastung des Hauptwärmetauschers auf den Einsatzmantel abzustützen.According to the invention, this effect can be further enhanced by that the rising fresh gas does not, as previously described, the individual catalyst containers washes around, but flows through the latter through centrally arranged passage openings. This can also be done on the peripheral annular space between the insert jacket and the catalyst tanks can be dispensed with, thereby gaining more catalyst space can be and the possibility is given, the catalyst container under discharge the exchanger pipes between these or with the main heat exchanger relieved to be supported on the insert jacket.

Diese zuletzt beschriebene Art der Gasführung durch zentrale Gasdurchlässe erlaubt daneben noch den Einbau von koaxialen Röhren vom unteren oder vom oberen Ofendeckel her für die Zuführung von kaltem Frischgas für den subtileren Temperaturspitzen-Ausgleich.This last-described type of gas flow through central gas passages also allows the installation of coaxial tubes from the lower or the upper Furnace lid for the supply of cold fresh gas for the more subtle compensation of temperature peaks.

Die oben beschriebene erfindungsgemäße Gasführung wird in Hochdruckreaktoren neuer Bauart durchgeführt, wie sie in den Fig. 1 und 2 der Zeichnung beispielsweise und im Prinzip dargestellt sind.The gas flow according to the invention described above is carried out in high pressure reactors carried out new design, as shown in Figs. 1 and 2 of the drawings, for example and are shown in principle.

1, 2 und 3 bedeuten den oberen und unteren Deckel und den Mantel des Druckmantels, 18 ist der Frischgaseinlaß durch eine Bohrung am Deckel 1; 19 ist der Ausgang für das zur Umsetzung gebrachte Synthesegas am unteren Ofendeckel, 4 der Einsatzmantel, der entweder durch eine Stopfbüchse mit dem Druckmanteldeckel l gasdicht abschließt (Fig. 1) oder aber oben durch einen Deckel geschlossen ist (Fig. 2). Dieses Einsatzrohr 4 weist in der Nähe des Bodens bzw. des unteren Endes des Hauptwärmetauschers 6 Gasdurchlässe 20 zum Hauptwärmetauscher 6 auf. Mit 7 bis 9 bzw. 10 sind die einzelnen Schüsse einer Mehrzahl von Katalysatorbehältern bezeichnet, die jeweils durch mehrere Austauscherrohre 11, die außen von dem im Gegenstrom passierenden Frischgas umspült werden, untereinander gasführend in Verbindung stehen. Der Frischgasstrom um diese Rohre 11 wird in an sich bekannter Weise durch Schikanenbleche geienkt. Bei 21 in Fig. 1 ist eine in bekannter Weise ausgestaltete elektrische Heizeinrichtung angedeutet, die in Fig. 2 durch den üblichen Brenner ersetzt ist. 15 in Fig. 1 ist der zusätzliche oder innere Ringraum zwischen Druckmantel 2 und den Wänden der Katalysatorbehälter 7 bis 10. Mit 12 in Fig. 2 sind die zentralen Durchlässe für das Frischgas durch die Katalysatorbehälter 7, B. 9 bezeichnet. Ebendort bedeutet 13 den Brenner, 17 das Umlenkrohr, 14 das Brennerrohr und 16 Kaltgaszuführungen zu den einzelnen Austauscherrohrsätzen 11 bzw. zum Hauptwärmetauscher 6. 1, 2 and 3 mean the upper and lower cover and the jacket of the pressure jacket, 18 is the fresh gas inlet through a hole in the cover 1; 19 is the outlet for the synthesis gas brought to implementation at the lower furnace cover, 4 the insert jacket, which is either sealed gas-tight by a stuffing box with the pressure jacket cover l (Fig. 1) or is closed at the top by a cover (Fig. 2). In the vicinity of the bottom or the lower end of the main heat exchanger 6, this insert tube 4 has gas passages 20 to the main heat exchanger 6. The individual sections of a plurality of catalyst containers are denoted by 7 to 9 or 10, each of which is connected to one another in a gas-carrying manner by a plurality of exchanger tubes 11 around which the fresh gas flowing in countercurrent flows. The fresh gas flow around these pipes 11 is deflected in a manner known per se by baffle plates. At 21 in Fig. 1, an electrical heating device designed in a known manner is indicated, which is replaced in Fig. 2 by the usual burner. 15 in Fig. 1 is the additional or inner annular space between the pressure jacket 2 and the walls of the catalyst container 7 to 10. With 12 in Fig. 2, the central passages for the fresh gas through the catalyst container 7, B. 9 are designated. There 13 means the burner, 17 the deflection tube, 14 the burner tube and 16 cold gas feeds to the individual exchanger tube sets 11 or to the main heat exchanger 6.

Claims (7)

PATENTANSPRÜCHE: 1. Verfahren zur Gasführung in katalytischen Hochdrucksyntheseanlagen mit zwei oder mehreren in einem Einsatzmantel übereinander angeordneten, im Gaswege miteinander verbundenen Katalysatorbehältern, dadurch gekennzeichnet, daß das an einem Ende des Ofens aufgegebene kalte Eingangsgasgemisch einen durch den Druckmantel (1, 2, 3) und den die Katalysatorbehälter umschließenden Einsatzmantel (4) gebildeten, an sich bekannten peripheren Ringraum (5) und sodann einen am entgegengesetzten Ende des Ofens befindlichen, ebenfalls an sich bekannten Hauptwärmeaustauscher (6) durchströmt, wonach es, teilweise aufgewärmt, innerhalb des Einsatzmantels (4) im Gegenstrom zum Eingangsgasstrom entweder nacheinander die Außenseite der Wände der einzelnen Katalysatorbehälter (7 bis 10) umströmt oder diese letzteren durch zentral angeordnete Gasdurchlässe (12) nacheinander durchströmt, wobei zwischen den einzelnen Katalysatorbehältern angeordnete und diese miteinander verbindende kurze Austauscherrohre (11) gekühlt werden, und das Gas anschließend auf die oberste Katalysatorlage (7) aufgegeben und in neuerlicher Umkehr der Strömungsrichtung die einzelnen Katalysatorbehälter (7 bis 10) und die Austauscherrohre (11) durchströmt und den Ofen durch den Hauptwärmeaustauscher (6) hindurch verläßt. CLAIMS: 1. A method for conducting gas in the catalytic high pressure synthesis systems with two or more superimposed in an insert shell arranged, connected to each other in the gas-way catalyst containers, characterized in that the checked at one end of the furnace cold inlet gas mixture has a through the pressure shell (1, 2, 3) and the peripheral annular space (5), which is known per se and which surrounds the catalyst container, flows through it and then a main heat exchanger (6) also known per se located at the opposite end of the furnace, whereupon it, partially warmed up, flows inside the insert jacket (4 ) in countercurrent to the inlet gas flow either successively flows around the outside of the walls of the individual catalyst containers (7 to 10) or flows through these latter one after the other through centrally arranged gas passages (12) , with short outs arranged between the individual catalyst containers and connecting them to one another exchanger tubes (11) are cooled, and the gas is then applied to the topmost catalyst layer (7) and, in a renewed reversal of the direction of flow, flows through the individual catalyst containers (7 to 10) and the exchanger tubes (11) and through the furnace through the main heat exchanger (6) leaves. 2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß der auf seinem Wege durch den Ringraum (5), den Hauptwärmeaustauscher (6) und um die Austauseherrohre (11) zwischen den einzelnen Katalysatorbehältern (7 bis 9) aufgewärmte Frischgasstrom unterhalb der obersten Katalysatorlage (7) umgelenkt und in bekannter Weise durch einen elektrischen Brenner (13) erhitzt wird. 2. The method according to claim 1, characterized in that the fresh gas stream warmed up on its way through the annular space (5), the main heat exchanger (6) and around the exchanger tubes (11) between the individual catalyst containers (7 to 9) below the top catalyst layer ( 7) is deflected and heated in a known manner by an electric burner (13). 3. Verfahren nach Anspruch 1 oder 2, dadurch gekennzeichnet, daß dem erfindungsgemäß vorgewärmten Frischgasstrom vor Eintritt in die erste Katalysatorlage (7) bzw. nach dem Verlassen des Hauptwärmeaustauschers (6) oder auf seinem Wege zwischen diesen beiden kaltes Frischgasgemisch regelbar zugesetzt wird. 3. The method according to claim 1 or 2, characterized in that the fresh gas stream preheated according to the invention before entry into the first catalyst layer (7) or after leaving the main heat exchanger (6) or on its way between these two cold fresh gas mixture is controllably added. 4. Vorrichtung zur Durchführung des Verfahrens nach Anspruch 1, bestehend aus einem Druckmantel (1 bis 3), einem die Katalysatorbehälter umschließenden, oben geschlossenen Einsatzmantel (4), einem endständigen Hauptwärmeaustauscher (6) und zwei oder mehreren hintereinander angeordneten und im Gaswege miteinander verbundenen Katalysatorbehältern (7 bis 10), dadurch gekennzeichnet, daß die einzelnen Kztalysatorbehälter (7 bis 10) durch je eine Mehrzahl Austauscherrohre (11) untereinander gasführend verbunden und so angeordnet sind, daß zwischen ihnen und dem Einsatzmantel ein Ringraum (15) gebildet wird. 4. Apparatus for performing the method according to claim 1, consisting of a pressure jacket (1 to 3), an insert jacket (4) which surrounds the catalyst container and which is closed at the top, a terminal main heat exchanger (6) and two or more successively arranged and interconnected in the gas path Catalyst tanks (7 to 10), characterized in that the individual catalyst tanks (7 to 10) are each connected to one another in a gas-carrying manner by a plurality of exchanger tubes (11) and are arranged in such a way that an annular space (15) is formed between them and the insert jacket. 5. Vorrichtung zur Durchführung des Verfahrens nach Anspruch], bestehend aus einem Druckmantel (1 bis 3), einem die Katalysatorbehälter umschließenden, oben geschlossenen Einsatzmantel (4), einem endständigen Hauptwärmeaustauscher (6) und zwei oder mehreren hintereinander angeordneten und miteinander gasführend verbundenen Katalysatorbehältern (7 bis 9), dadurch gekennzeichnet, daß die einzelnen Katalysatorbehälter (7 bis 9) einerseits durch je eine Mehrzahl kurzer Austauscherrohre (11) untereinander verbunden sind und andererseits die Katalysatorbehälter (7 bis 9) unter gasdichtem peripherem Anschluß an den Einsatzmantel (4) untereinander korrespondierende, zentral angeordnete Gasdurchlässe (12) aufweisen. 5. Apparatus for performing the method according to claim], consisting of a pressure jacket (1 to 3), an insert jacket (4) which surrounds the catalyst container and which is closed at the top, a terminal main heat exchanger (6) and two or more catalyst containers arranged one behind the other and connected to one another in a gas-carrying manner (7 to 9), characterized in that the individual catalyst containers (7 to 9) are connected to one another on the one hand by a plurality of short exchanger tubes (11) each and on the other hand the catalyst containers (7 to 9) with a gas-tight peripheral connection to the insert casing (4) have mutually corresponding, centrally arranged gas passages (12). 6. Vorrichtung nach Anspruch 5, dadurch gekennzeichnet, daß innerhalb der miteinander korrespondierenden zentralen Gasdurchlässe (12) in an sich bekannter Weise koaxiale Rohre (16) zur Frischgaszuführung angeordnet sind. 6. Apparatus according to claim 5, characterized in that within the mutually corresponding central gas passages (12) coaxial tubes (16) are arranged in a manner known per se for supplying fresh gas. 7. Vorrichtung nach Anspruch 5, gekennzeichnet durch ein koaxial um das Brennerrohr (14) angeordnetes Umlenkrohr (17). In Betracht gezogene Druckschriften: Deutsche Patentschriften Nr. 926 366, 566 577, 263 287; . deutsche Auslegeschriften Nr. 1052 958, 1009 602; USA.-Patentschrift Nr. 2 538 738.7. Apparatus according to claim 5, characterized by a deflection tube (17) arranged coaxially around the burner tube (14). Considered publications: German Patent Nos. 926 366, 566 577, 263 287; . German Auslegeschriften No. 1052 958, 1009 602; U.S. Patent No. 2,538,738.
DEL37594A 1965-01-29 1960-11-22 Process and device for gas supply in catalytic high pressure reactors Pending DE1142586B (en)

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DE1210422B (en) * 1963-03-01 1966-02-10 Metallgesellschaft Ag Process for heating and cooling down sulfur-acid contact systems
US3440021A (en) * 1966-07-05 1969-04-22 Chemie Linz Ag High pressure reactor
US3472631A (en) * 1966-04-25 1969-10-14 Robert H Schober Apparatus for carrying out exothermic catalytic gas reactions
DE1542517B1 (en) * 1965-08-25 1972-01-05 Ube Industries Furnace for high pressure catalytic synthesis
DE2710247A1 (en) * 1976-03-10 1977-09-22 Topsoe Haldor As PROCEDURE FOR AMMONIA SYNTHESIS AND CONVERTER FOR THIS
DE3040712A1 (en) * 1980-10-29 1982-05-27 W.C. Heraeus Gmbh, 6450 Hanau Reaction vessel esp. for high temp. high pressure catalysis - has temp. resistant inner shell pressure resistant outer shell and insulation between
DE3146778A1 (en) * 1980-11-28 1982-08-19 Ammonia Casale S.A., 6900 Lugano AXIAL-RADIAL-REACTOR FOR HETEROGENEOUS SYNTHESIS
DE3336750A1 (en) * 1982-10-15 1984-04-19 Idemitsu Kosan Co., Ltd., Tokyo REACTOR
EP1707259A1 (en) * 2005-04-01 2006-10-04 Methanol Casale S.A. Reactor for the heterogeneous synthesis of chemical compounds

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US2538738A (en) * 1945-09-04 1951-01-16 Commercial Solvents Corp Process and apparatus for carrying out exothermic reactions
DE926366C (en) * 1952-07-25 1955-04-14 Basf Ag High pressure furnace for carrying out catalytic gas reactions
DE1009602B (en) * 1954-03-18 1957-06-06 Montedison Spa Process for carrying out exothermic catalytic gas reactions under high pressure and at high temperature
DE1052958B (en) * 1956-07-21 1959-03-19 Uhde Gmbh Friedrich Device for carrying out catalytic high pressure syntheses

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DE566577C (en) * 1925-02-16 1932-12-22 Giovanni Cicali Device for the synthetic production of ammonia by catalysis
US2538738A (en) * 1945-09-04 1951-01-16 Commercial Solvents Corp Process and apparatus for carrying out exothermic reactions
DE926366C (en) * 1952-07-25 1955-04-14 Basf Ag High pressure furnace for carrying out catalytic gas reactions
DE1009602B (en) * 1954-03-18 1957-06-06 Montedison Spa Process for carrying out exothermic catalytic gas reactions under high pressure and at high temperature
DE1052958B (en) * 1956-07-21 1959-03-19 Uhde Gmbh Friedrich Device for carrying out catalytic high pressure syntheses

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1210422B (en) * 1963-03-01 1966-02-10 Metallgesellschaft Ag Process for heating and cooling down sulfur-acid contact systems
DE1542517B1 (en) * 1965-08-25 1972-01-05 Ube Industries Furnace for high pressure catalytic synthesis
US3472631A (en) * 1966-04-25 1969-10-14 Robert H Schober Apparatus for carrying out exothermic catalytic gas reactions
US3440021A (en) * 1966-07-05 1969-04-22 Chemie Linz Ag High pressure reactor
DE2710247A1 (en) * 1976-03-10 1977-09-22 Topsoe Haldor As PROCEDURE FOR AMMONIA SYNTHESIS AND CONVERTER FOR THIS
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DE3040712A1 (en) * 1980-10-29 1982-05-27 W.C. Heraeus Gmbh, 6450 Hanau Reaction vessel esp. for high temp. high pressure catalysis - has temp. resistant inner shell pressure resistant outer shell and insulation between
DE3146778A1 (en) * 1980-11-28 1982-08-19 Ammonia Casale S.A., 6900 Lugano AXIAL-RADIAL-REACTOR FOR HETEROGENEOUS SYNTHESIS
DE3336750A1 (en) * 1982-10-15 1984-04-19 Idemitsu Kosan Co., Ltd., Tokyo REACTOR
EP1707259A1 (en) * 2005-04-01 2006-10-04 Methanol Casale S.A. Reactor for the heterogeneous synthesis of chemical compounds

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