CH384125A - Catalytic conversion plant for the continuous generation of gases of all kinds from hydrocarbons - Google Patents

Catalytic conversion plant for the continuous generation of gases of all kinds from hydrocarbons

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Publication number
CH384125A
CH384125A CH610861A CH610861A CH384125A CH 384125 A CH384125 A CH 384125A CH 610861 A CH610861 A CH 610861A CH 610861 A CH610861 A CH 610861A CH 384125 A CH384125 A CH 384125A
Authority
CH
Switzerland
Prior art keywords
annular space
tubes
forming
gases
hydrocarbons
Prior art date
Application number
CH610861A
Other languages
German (de)
Inventor
Mertens Carl
Original Assignee
Mertens Carl
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 Mertens Carl filed Critical Mertens Carl
Publication of CH384125A publication Critical patent/CH384125A/en

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    • 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
    • C01B3/382—Multi-step processes
    • 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
    • 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
    • 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
    • C01B3/386—Catalytic partial combustion
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/20—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours
    • C10G11/22—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert heated gases or vapours produced by partial combustion of the material to be cracked
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C10G9/38—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours produced by partial combustion of the material to be cracked or by combustion of another hydrocarbon
    • 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
    • B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
    • 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
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Description

  

  
 



  Katalytische Umformungsanlage zur kontinuierlichen Erzeugung von Gasen aller Art aus Kohlenwasserstoffen
Die Erfindung betrifft eine katalytische Umformungsanlage zur kontinuierlichen Erzeugung von Gasen aller Art, wie Stadtgas, Synthesegas oder olefinreicher Gase zur chemischen Weiterverarbeitung, aus Kohlenwasserstoffen z. B. mit Reaktionspartnern, wie Luft, Sauerstoff und Wasserdampf, einzeln oder in bestimmten Verhältnissen zugeführt. Bekannte Anlagen dieser Art haben den Nachteil, dass sie grosse Wärmemengen sowohl zur Vorwärmung des Einsatzgemisches als auch zur Durchführung der Reaktion und lange Kontaktrohre benötigen.



   Der Erfindung liegt die Aufgabe zugrunde, eine katalytische Umformungsanlage zu schaffen, die bei gedrungener Bauart und geringem Aufwand an zugeführter Wärme mit grossem Wirkungsgrad arbeitet.



   Erfindungsgemäss wird die Aufgabe dadurch gelöst, dass ein Umformungselement mit einem Wärmeaustauscher, einem Prozessluftvorwärmer und einem Brenner zu einer Einheit zusammengefasst ist, die über eine Flanschverbindung mit einem Prozessdampferzeuger lösbar verbunden ist. Diese Anordnung hat den Vorteil, dass das Umformungselement leicht ausgewechselt werden kann und etwaige Reparaturen oder Erneuerungen ohne Störung benachbarter Anlagen durchgeführt werden können.



   Zur Erhöhung der Heizfläche können die Rohre des Umformungselementes gerippt oder gewellt ausgeführt sein.



   In der Zeichnung ist ein Ausführungsbeispiel der Anlage nach der Erfindung dargestellt, und zwar zeigt:
Fig. 1 die Anlage im Axialschnitt,
Fig. 2 einen Schnitt nach der Linie A-A' in Fig. 1 und
Fig. 3 einen Schnitt nach der Linie   B-B' in    Fig. 1.



   Die gezeichnete katalytische Umformungsanlage besteht aus einem Umformungselement 1, einem Wärmeaustauscher 2, einem Prozessluftvorwärmer 3, einem Brenner 4 und einem Prozessdampferzeuger 5.



  Dabei sind Umformungselement 1, Wärmeaustauscher 2, Prozessluftvorwärmer 3 und Brenner 4 zu einer Einheit zusammengefasst und mit dem Prozessdampferzeuger 5 über eine Flanschverbindung 6 lösbar verbunden. Das Umformungselement 1 besteht aus drei konzentrisch zueinander angeordneten Rohren 7, 8 und 9, die zwei Ringräume 10 und 11 bilden.



  Die Ringräume 10 und 11 sind unten miteinander verbunden und mit Katalysatormasse gefüllt. An die Ringräume 10 und 11 schliesst sich oben der Wärmeaustauscher 2 an. Der Wärmeaustauscher 2 besteht aus zwei zueinander konzentrischen Rohren 12 und 13, die einen Ringraum 14 bilden, der oben geschlossen, mit einem Stutzen 15 versehen und unten mit dem Ringraum 10 verbunden ist. Im Ringraum 14 sind Rohre 16 auf einem Kreise angeordnet, die unten mit dem Ringraum 11 und oben mit einem Raum 17 von kreisförmigem Querschnitt in Verbindung stehen.



  Der Wärmeaustauscher 2 ist von dem Luftvorwärmer 3 umgeben. In seinem Innenraum befindet sich der Brenner 4, in dem ein geeigneter Brennstoff mit Luft zu Rauchgas verbrannt wird. Der Luftvorwärmer 3 besteht aus drei konzentrisch angeordneten Rohren 18, 19 und 20, die oben und unten geschlossen sind.



  Sie bilden zwei Ringräume 21 und 22, die unten miteinander verbunden und mit   Ein- und    Austrittsstutzen 23 und 24 versehen sind. Der Prozessdampferzeuger 5 besteht aus vier konzentrisch angeordneten Rohren 25, 26, 27 und 28, die oben und unten geschlossen sind. Sie bilden drei Ringräume 29, 30 und 31. In das innere Rohr 28 ragt das Umformungselement 1  hinein. Der äussere Ringraum 29 ist mit einem Stutzen 32 zum Austritt der Rauchgase, der mittlere Ringraum 30 mit einem Stutzen 33 zum Austritt des Prozessdampfes und mit einem Stutzen 34 zum Eintritt des Speisewassers versehen. Am Boden der Rohre 26 und 27 sind Verbindungen 35 zwischen dem inneren Ringraum 31 und dem äusseren Ringraum 29 angeordnet. Ein Stutzen 36 im Boden des Rohres 26 dient zur Abschlämmung des Prozessdampferzeugers 5.



   Bei Betrieb der Anlage tritt die Prozessluft durch den tangential angeordneten Stutzen 23 in den Prozessluftvorwärmer 3 mit einer Temperatur von 20 bis   35o C    ein, verlässt diesen, auf etwa   2000 C    vorgewärmt, durch den Stutzen 24 und wird mit aus dem Stutzen 33 austretenden Prozessdampf gemischt. Die Kohlenwasserstoffmenge wird dosiert in dieses Gemisch eingespeist. Das Gemisch Prozessluft-Wasserdampf-Kohlenwasserstoff tritt durch den Stutzen 15 in den Ringraum 14 des Wärmeaustauschers 2 ein, um durch die heissen, im Gegenstrom durch die Rohre 16 fliessenden Umformungsgase auf eine Temperatur von 450 bis   500     C vorgewärmt zu werden.

   Mit dieser Temperatur tritt das Umformungsgemisch in den mit Katalysator gefüllten äusseren Ringraum 10 des Umformungselementes 1 ein und setzt sich hier zunächst vornehmlich mit der Prozessluft und geringer Wasserdampfumformung teilweise in Umformungsgas um. Die Heizung erfolgt durch Rauchgase, die in dem durch die Rohre 7 und 28 gebildeten Ringraum 37 im Gegenstrom nach oben ziehen. Die Rauchgase tauschen sich hier von etwa 9000 C unten bis   750"    C oben aus. Die fühlbare Wärme der Rauchgase wird durch das Aussenrohr 7 des Umformungselementes 1 in dem Ringraum 10 zur Unterstützung der Umformung abgeführt. Die Umformungsgase und unzersetzten Kohlenwasserstoffe im Gemisch mit Wasserdampf treten zur Endumsetzung der noch unzersetzten Kohlenwasserstoffe mit Wasserdampf aus dem Ringraum 10 in den Ringraum 11, der gleichfalls mit Katalysator gefüllt ist.

   Diese Reaktion verbraucht viel Wärme, die grösstenteils durch direkte Beheizung des Innenrohres 9 aus der den Brenner 4 verlassenden Strahlungswärme der Rauchgase abgedeckt wird. Das fertige Umformungsgas verlässt den Ringraum 11 und tritt in die konzentrisch angeordneten Rohre des Wärmeaustauschers 2 ein. Hier wird der grösste Teil der fühlbaren Wärme zur Temperaturerhöhung des Einsatzgemisches indirekt in den Wärmeaustauscher 2 abgegeben. Das gekühlte Umformungsgas tritt bei 38 tangential aus.



   Die durch den Brenner 4 erzeugten Rauchgase geben die für die Umsetzung vornehmlich über die Wasserdampfreaktion benötigte Wärme an den mit Katalysator gefüllten Ringraum 11 im Gegenstrom ab. Sie kehren unten um, um im Ringraum 37 im Gegenstrom gegen das Einsatzgemisch die notwendige Wärme mittelbar an das Einsatzprodukt im Ringraum 10 abzugeben. Die Rauchgase treten nach Abdeckung der gesamten Umformungswärme und anteiligen Prozessluftvorwärmung in den Ringraum 31 ein, um einen Teil ihrer fühlbaren Wärme an den Prozessdampferzeuger 5 abzugeben. Dieser Prozessdampferzeuger ist zweiseitig mit Rauchgas zur Verdampfung des Wassers umspült, das sich im Ringraum 30 befindet. Aus dem Ringraum 31 treten die Rauchgase durch die Verbindungen 35 in den Ringraum 29 über, beheizen den Ringraum 30 und treten durch den Stutzen 32 in die Atmosphäre aus.

   Der Prozess dampf verlässt den Dampferzeuger durch den Stutzen 34. Die Prozessluft tritt durch den Stutzen 23 in den Prozessluftvorwärmer 3 ein, durchströmt den Ringraum 21 und im Gegenstrom den Ringraum 22 und verlässt den Vorwärmer 3 durch den Stutzen 24.



   Trotz der hohen Temperaturen ist eine feuerfeste Auskleidung nicht erforderlich, weil die oberen Partien im Luftvorwärmer 3 kühl gehalten werden.   



  
 



  Catalytic conversion plant for the continuous generation of gases of all kinds from hydrocarbons
The invention relates to a catalytic conversion system for the continuous generation of gases of all kinds, such as town gas, synthesis gas or olefin-rich gases for chemical processing, from hydrocarbons z. B. with reactants such as air, oxygen and steam, supplied individually or in certain proportions. Known systems of this type have the disadvantage that they require large amounts of heat both to preheat the feed mixture and to carry out the reaction and require long contact tubes.



   The invention is based on the object of creating a catalytic conversion system which, with a compact design and little expenditure on supplied heat, operates with great efficiency.



   According to the invention, the object is achieved in that a deformation element with a heat exchanger, a process air preheater and a burner is combined to form a unit which is detachably connected to a process steam generator via a flange connection. This arrangement has the advantage that the deformation element can easily be exchanged and any repairs or renewals can be carried out without disrupting neighboring systems.



   To increase the heating surface, the tubes of the forming element can be ribbed or corrugated.



   In the drawing, an embodiment of the system according to the invention is shown, namely shows:
1 shows the system in axial section,
Fig. 2 shows a section along the line A-A 'in Fig. 1 and
3 shows a section along line B-B 'in FIG.



   The depicted catalytic conversion system consists of a conversion element 1, a heat exchanger 2, a process air preheater 3, a burner 4 and a process steam generator 5.



  The deformation element 1, heat exchanger 2, process air preheater 3 and burner 4 are combined to form a unit and are releasably connected to the process steam generator 5 via a flange connection 6. The deformation element 1 consists of three tubes 7, 8 and 9 which are arranged concentrically to one another and which form two annular spaces 10 and 11.



  The annular spaces 10 and 11 are connected to one another at the bottom and filled with catalyst mass. The heat exchanger 2 adjoins the annular spaces 10 and 11 at the top. The heat exchanger 2 consists of two tubes 12 and 13 which are concentric to one another and which form an annular space 14 which is closed at the top, is provided with a nozzle 15 and is connected to the annular space 10 at the bottom. In the annular space 14, tubes 16 are arranged on a circle, which are connected at the bottom with the annular space 11 and at the top with a space 17 of circular cross-section.



  The heat exchanger 2 is surrounded by the air preheater 3. In its interior is the burner 4, in which a suitable fuel is burned with air to form flue gas. The air preheater 3 consists of three concentrically arranged tubes 18, 19 and 20 which are closed at the top and bottom.



  They form two annular spaces 21 and 22 which are connected to one another at the bottom and are provided with inlet and outlet nozzles 23 and 24. The process steam generator 5 consists of four concentrically arranged tubes 25, 26, 27 and 28 which are closed at the top and bottom. They form three annular spaces 29, 30 and 31. The deformation element 1 protrudes into the inner tube 28. The outer annular space 29 is provided with a connector 32 for the exit of the flue gases, the middle annular space 30 with a connector 33 for the exit of the process steam and with a connector 34 for the entry of the feed water. At the bottom of the tubes 26 and 27, connections 35 are arranged between the inner annular space 31 and the outer annular space 29. A connecting piece 36 in the bottom of the pipe 26 serves to blow down the process steam generator 5.



   When the system is in operation, the process air enters the process air preheater 3 through the tangentially arranged nozzle 23 at a temperature of 20 to 35o C, leaves it, preheated to around 2000 C, through the nozzle 24 and is mixed with the process steam emerging from the nozzle 33 . The amount of hydrocarbons is metered into this mixture. The mixture of process air, water vapor and hydrocarbons enters the annular space 14 of the heat exchanger 2 through the nozzle 15, in order to be preheated to a temperature of 450 to 500 C by the hot forming gases flowing in countercurrent through the tubes 16.

   At this temperature, the forming mixture enters the catalyst-filled outer annular space 10 of the forming element 1 and is initially partially converted into forming gas, primarily with the process air and a slight amount of steam forming. The heating takes place by means of flue gases which pull upwards in countercurrent in the annular space 37 formed by the tubes 7 and 28. The flue gases exchange here from about 9000 C below to 750 "C above. The sensible heat of the flue gases is dissipated through the outer tube 7 of the shaping element 1 in the annular space 10 to support the shaping for the final conversion of the still undecomposed hydrocarbons with water vapor from the annular space 10 into the annular space 11, which is also filled with catalyst.

   This reaction consumes a lot of heat, which is largely covered by direct heating of the inner tube 9 from the radiant heat of the flue gases leaving the burner 4. The finished reforming gas leaves the annular space 11 and enters the concentrically arranged tubes of the heat exchanger 2. Here, the major part of the sensible heat for increasing the temperature of the feed mixture is given off indirectly into the heat exchanger 2. The cooled reforming gas exits at 38 tangentially.



   The flue gases generated by the burner 4 give off the heat required for the conversion, primarily via the steam reaction, to the annular space 11 filled with catalyst in countercurrent. They turn around at the bottom in order to transfer the necessary heat indirectly to the input product in the annular space 10 in countercurrent against the feed mixture in the annular space 37. After covering the entire deformation heat and partial process air preheating, the flue gases enter the annular space 31 in order to give off part of their sensible heat to the process steam generator 5. This process steam generator is surrounded on two sides with flue gas to evaporate the water that is located in the annular space 30. From the annular space 31, the flue gases pass through the connections 35 into the annular space 29, heat the annular space 30 and exit through the nozzle 32 into the atmosphere.

   The process steam leaves the steam generator through the nozzle 34. The process air enters the process air preheater 3 through the nozzle 23, flows through the annular space 21 and countercurrently through the annular space 22 and leaves the preheater 3 through the nozzle 24.



   Despite the high temperatures, a refractory lining is not required because the upper parts in the air preheater 3 are kept cool.

Claims (1)

PATENTANSPRUCH Katalytische Umformungsanlage zur kontinuierlichen Erzeugung von Gasen aller Art aus Kohlenwasserstoff, dadurch gekennzeichnet, dass ein Umformungselement (1) mit einem Wärmeaustauscher (2), einem Prozessluftvorwärmer (3) und einem Brenner (4) zu einer Einheit zusammengefasst ist, die über eine Flanschverbindung (6) mit einem Prozessdampferzeuger (5) lösbar verbunden ist. PATENT CLAIM Catalytic conversion system for the continuous generation of gases of all kinds from hydrocarbons, characterized in that a conversion element (1) with a heat exchanger (2), a process air preheater (3) and a burner (4) is combined to form a unit which is connected via a flange connection ( 6) is detachably connected to a process steam generator (5). UNTERANSPRÜCHE 1. Umformungsanlage nach Patentanspruch, dadurch gekennzeichnet, dass das Umformungselement (1) aus drei konzentrisch zueinander angeordneten Rohren (7, 8, 9) besteht, die zwei unten miteinander verbundene und mit Katalysatormasse gefüllte Ringräume (10, 11) bilden und mit denen der Wärmeaustauscher (2) verbunden ist, der aus konzentrisch angeordneten Rohren (12, 13) besteht, die einen Ringraum (14) bilden, in dem Rohre (16) kreisförmig angeordnet sind, der von dem Luftvorwärmer (3) umgeben ist und in dessen Innenraum sich der Brenner (4) befindet. SUBCLAIMS 1. Forming plant according to claim, characterized in that the forming element (1) consists of three concentrically arranged tubes (7, 8, 9) which form two annular spaces (10, 11) which are connected at the bottom and are filled with catalyst mass and with which the Heat exchanger (2) is connected, which consists of concentrically arranged tubes (12, 13) which form an annular space (14) in which tubes (16) are arranged in a circle, which is surrounded by the air preheater (3) and in its interior the burner (4) is located. 2. Umformungsanlage nach Unteranspruch 1, dadurch gekennzeichnet, dass der Luftvorwärmer (3) aus drei konzentrisch zueinander angeordneten, oben und unten geschlossenen, zwei Ringräume (21, 22) bildenden Rohren (18, 19, 20) besteht, wobei die Ringräume (21, 22) unten miteinander verbunden und oben mit je einem Stutzen (23, 24) verbunden sind. 2. Forming plant according to dependent claim 1, characterized in that the air preheater (3) consists of three tubes (18, 19, 20) which are arranged concentrically to one another and are closed at the top and bottom and form two annular spaces (21, 22), the annular spaces (21 , 22) are connected to each other at the bottom and each connected to a connecting piece (23, 24) at the top. 3. Umformungsanlage nach Unteranspruch 2, dadurch gekennzeichnet, dass der Prozessdampferzeuger (5) aus vier konzentrisch zueinander angeordneten, unten und oben geschlossenen, drei Ringräume (29, 30, 31) bildenden Rohren (25, 26, 27, 28) besteht, in die das Umformungselement (1) hineinragt, wobei der äussere Ringraum (29) mit einem Stutzen (32) zum Austritt der Rauchgase und der mittlere Ringraum (30) mit einem Stutzen (33) zum Austritt des Prozessdampfes und einem Stutzen (34) zum Eintritt des Speisewassers versehen ist, und am Boden Ver bindungen (35) zwischen dem inneren (31) und dem äusseren Ringraum (29) angeordnet sind. 3. Forming plant according to dependent claim 2, characterized in that the process steam generator (5) consists of four concentrically arranged tubes (25, 26, 27, 28) which are closed at the bottom and top and form three annular spaces (29, 30, 31), in which the deformation element (1) protrudes, the outer annular space (29) with a connection (32) for the exit of the smoke gases and the middle annular space (30) with a connection (33) for the exit of the process steam and a connection (34) for the entry of the feed water is provided, and connections (35) between the inner (31) and the outer annular space (29) are arranged on the ground. 4. Umformungsanlage nach Unteranspruch 3, dadurch gekennzeichnet, dass die das Umformungselement (1) bildenden Rohre (7, 8, 9) horizontal oder vertikal gerippt oder gewellt ausgeführt sind. 4. Forming plant according to dependent claim 3, characterized in that the tubes (7, 8, 9) forming the forming element (1) are horizontally or vertically ribbed or corrugated.
CH610861A 1960-06-02 1961-05-25 Catalytic conversion plant for the continuous generation of gases of all kinds from hydrocarbons CH384125A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
DEM45518A DE1093948B (en) 1960-06-02 1960-06-02 Catalytic conversion plant for the continuous generation of gases of all kinds from hydrocarbons

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CH384125A true CH384125A (en) 1964-11-15

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BE (1) BE604181A (en)
CH (1) CH384125A (en)
DE (1) DE1093948B (en)
FR (1) FR1292477A (en)
GB (1) GB954844A (en)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1143295B (en) * 1961-05-06 1963-02-07 Metallgesellschaft Ag Device for the autothermal, catalytic cracking of hydrocarbons under pressure
DE1197187B (en) * 1962-12-11 1985-07-27 Pintsch Bamag Ag Device for splitting hydrocarbons for the production of a city or industrial gas
US4071330A (en) * 1976-12-22 1978-01-31 United Technologies Corporation Steam reforming process and apparatus therefor
US4861347A (en) * 1986-12-29 1989-08-29 International Fuel Cells Corporation Compact chemical reaction vessel
GB9217685D0 (en) * 1992-08-20 1992-09-30 British Petroleum Co Plc Process for the production of mono-olefins
GB2359764A (en) 2000-03-01 2001-09-05 Geoffrey Gerald Weedon An endothermic tube reactor

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GB954844A (en) 1964-04-08
DE1093948B (en) 1960-12-01
BE604181A (en) 1961-09-18
FR1292477A (en) 1962-05-04

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