EP0609191B1 - Apparatus for the thermal cracking of a mixture of liquid and gaseous hydrocarbons - Google Patents

Apparatus for the thermal cracking of a mixture of liquid and gaseous hydrocarbons Download PDF

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Publication number
EP0609191B1
EP0609191B1 EP94890007A EP94890007A EP0609191B1 EP 0609191 B1 EP0609191 B1 EP 0609191B1 EP 94890007 A EP94890007 A EP 94890007A EP 94890007 A EP94890007 A EP 94890007A EP 0609191 B1 EP0609191 B1 EP 0609191B1
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EP
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Prior art keywords
heat exchanger
mixture
line
liquid
gas
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EP94890007A
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German (de)
French (fr)
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EP0609191A1 (en
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Peter Dipl.-Ing. Illyes
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OMV Downstream GmbH
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OMV AG
OEMV AG
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    • 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
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means

Definitions

  • the invention relates to a device for thermal splitting of a mixture with liquid and gaseous hydrocarbons in heat exchangers.
  • gaseous hydrocarbons are also used. These gaseous hydrocarbons come from mostly from the processing facilities according to Splitting plants or production plants for the most varied Product blends. This gaseous Products are usually delivered to the slitting line leading supply lines for the liquid hydrocarbons initiated. As a result, the range of uses of the Plant significantly increased and on the other hand occurs a substantial reduction in piping since parallel pipelines, u. for the gaseous Hydrocarbons and the liquid hydrocarbons, can be avoided.
  • the hydrocarbon mixtures usually need to be in several stages up to the temperature of the thermal Cleavage to be heated.
  • the throughput in each Stages, d. H. the heat exchangers is usually by volume, especially in the first stage, on partial evaporation of liquid hydrocarbons.
  • the device according to the invention for thermal splitting a mixture of liquid and gaseous hydrocarbons, with at least one pipe for that Mixture opens into a heat exchanger, which if necessary with one leading out of the heat exchanger Pipeline through a detour line with one in flow controllable shut-off device is fluidly connected, and the pipeline leading from the heat exchanger into which at least one more pipe for overheated Water vapor flows into another Heat exchanger opens, the output line in one downstream heat exchanger, if necessary with Catalyst, opens, the outlet line in a cooling and Splitting device opens, essentially exists in that seen in the direction of flow before Heat exchanger at least one gas separator for the Separation of a gaseous fraction from the mixture is provided, the detour line being a gas line, which has a shut-off device which can be regulated in the flow, from the gas separator into another heat exchanger, in particular via the further pipeline.
  • the gaseous in front of the first heat exchanger Portion separated from the starting product mixture double supply lines for the liquid or gaseous starting products can be avoided. Furthermore a mixture enters the heat exchanger, which can be essentially gas-free, so that the preferred Heat exchange to the liquid products can take place which due to the higher specific heat of Liquids are particularly effective against gases can.
  • the gas can pass through a gas separator Pipeline either in the further heat exchanger or already opens into the actual cracking furnace, be led.
  • the gas line thus serves as a detour line for the first heat exchanger, which also means the temperature the heat exchange medium, e.g. B. flue gases controlled can be. On the one hand, this allows a particularly high Heat exchange can be achieved, on the other hand one too great cooling, e.g. B. the flue gases, and thus one Falling below the dew point temperature and thus occurring corrosion can be avoided.
  • gas separator is designed as a gravity separator, so can be a simple one without great pressure loss Separation of the gaseous components from the gas / liquid mixture respectively.
  • a particularly effective separation between gas and Liquid can be done via a cyclone.
  • the gas line opens into the gas separator Flow direction seen before the further line for the Water vapor in the outgoing pipe from the heat exchanger, so can already in the further heat exchanger a product mixture of the liquid hydrocarbons, the gaseous hydrocarbons and water vapor occur so that the partial steam lowering in the Heat exchanger is taken into account particularly cheaply, which makes the liquid hydrocarbons particularly quick can evaporate and another high absorption of heat is achieved in this heat exchanger.
  • the gas line flows from the gas separator into the downstream heat exchanger, i.e. in the cracking furnace, especially in the output line from the rest Heat exchanger, so with a particularly large range of gaseous products in the mixture also in the further Heat exchanger a heat transfer without disadvantageous Influencing the gaseous starting products achieved will.
  • the gas line flows from the gas separator into the other Pipe for the water vapor, so a mixture of Water vapor and gaseous products can be achieved in turn then into the supply line for the further Heat exchanger can be initiated.
  • the gas line flows out of the gas separator into one Steam superheater, so the gas along with the water vapor be heated.
  • a shut-off device which can be regulated in the flow, provided by the pipeline after the Gas separator, which opens into the heat exchanger, branches off, and preferably in the further pipeline after the Confluence of the gas pipeline, so can also bursty oversupply of liquid hydrocarbons without pressure overload of the heat exchanger intercepted and controlled if necessary.
  • Heat exchangers can also be used as groups of heat exchangers be constructed.
  • the pipes R 1 and R 2 which conduct liquid hydrocarbons (gasoline) or gaseous hydrocarbons with two to four carbon atoms, lead to the pipe R 3 , which in turn opens into the gas separator G.
  • the liquid products are then passed through the pipe R 3 into the heat exchanger W 1 .
  • the gaseous products from the gas separator G pass through the gas line G 1 , which serves as a detour line for the heat exchanger W 1 , into the pipeline R 4 leading from the heat exchanger W 1 .
  • a steam line D 1 which forwards the steam from the steam superheater D, also opens into this pipeline R 4 .
  • the further heat exchanger W 2 in which the pipeline R 4 opens, is connected via an output line R 5 to the cracking furnace, the downstream heat exchanger S.
  • a pipe R 6 leads from the heat exchanger S into a cooling and separation device K + A.
  • the steam superheater D in which steam is optionally generated, the cracking furnace, the heat exchanger S and the heat exchangers W 1 and W 2 are designed as shell-and-tube heat exchangers, with flue gas serving as the heat transfer medium.
  • a valve V 1 which can be regulated in the flow can be provided in the gas line G 1 and is closed when it is desired that the entire product mixture is passed through the pipe R 3 into the heat exchanger W 1 .
  • a gas line G 2 can also lead into the outlet line R 5 of the heat exchanger W 2 , or, like the gas line G 3, also lead directly into the cracking furnace, the heat exchanger S.
  • These gas lines can have valves V 2 and V 3 which can be regulated in the flow.
  • the gas can be fed via a line G 4 to the steam superheater D or, if appropriate, to a steam generator.
  • a further detour line U 1 can also be provided, which branches off from the pipe line R 3 in front of the heat exchanger W 1 and opens into the pipe line R 4 after the heat exchanger W 1 .
  • This detour line U 1 has a flow controllable valve V 4 .
  • the heat exchangers W 1 and W 2 as well as the steam superheater D and the cracking furnace, the heat exchanger S are successively flowed through by flue gases, which serve as heat exchange medium.
  • the flue gases pass according to arrow X 1 through the cracking furnace, the heat exchanger S, then into a high-pressure steam superheater, not shown, in which high-pressure steam can be generated, which does not have to be fed to the process.
  • the flue gas then enters the steam superheater D according to the arrow X 3, in which process steam is introduced according to the arrow Z.
  • the flue gas From the steam superheater D, the flue gas enters according to the arrow X 4 into the heat exchanger W 2 , from which it can enter a boiler feed water preheater, not shown, which is also not required in the process according to the invention. From this preheating, the flue gas enters the heat exchanger W 1 according to arrow X 6 , from which the flue gases are then fed to the chimney according to arrow X 7 .
  • the arrangement of the heat exchangers is carried out in accordance with the required heat potential, the cracking furnace, the heat exchanger S requiring the highest temperature of the flue gases, whereas the heat exchanger W 1 requires flue gases with a much lower temperature.
  • the gas separator G shown schematically in FIG. 2 has a cylindrical tube 1 which serves as an outer container.
  • the pipeline R 3 into which the product mixture is introduced in liquid and gaseous form, opens into this outer container.
  • the cylindrical tube 1 there is an extreme slowdown in the flow velocity, at the same time a separation of the gaseous and the liquid phase occurs.
  • the liquid phase is discharged via the exiting pipeline R 3
  • the gaseous phase is discharged via the cylindrical pipe 2, which continues into the gas line G 1 , and thus reaches the pipeline R 4 with the valve V 1 open.
  • FIG. 3 there is a cyclone, the pipe R 3 opening tangentially into the conical container 3.
  • the product mixture moves downwards in a spiral along the outer container wall and separates.
  • the liquid phase is withdrawn via the pipeline R 3 located on the bottom, whereas the gaseous phase is withdrawn via the gas line G 1 .
  • the incoming product mixture was heated to 440 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way is then passed through the pipe R 5 with a nominal diameter of 80 mm into the cracking furnace S.
  • the cracking furnace is designed as a heat exchanger in which the mixture has been heated further.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .
  • a gas separator with a gas line G 1 was provided.
  • the product mixture entering the heat exchanger W 1 had a temperature of 60 ° C.
  • heating to 220 ° C occurred.
  • 15 vol .-% of the gaseous phase and no portion of the liquid phase of the product were passed through the gas line G 1 , which was therefore not heated.
  • the product mixture then reached the pipeline R 4 , into which water vapor at 483 ° C. and in an amount of 1,300 kg / h with a nominal width of 80 mm was introduced into the heat exchanger W 2 .
  • the incoming product mixture was heated to 450 ° C in the heat exchanger W 2 .
  • the product mixture heated in this way was then fed into the cracking furnace S via the pipeline R 5 with a nominal diameter of 80 mm. Heating was also carried out in the cracking furnace itself.
  • a mixture at 855 ° C. emerged from the pipeline R 6 .

Description

Die Erfindung bezieht sich auf eine Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen in Wärmetauschern.The invention relates to a device for thermal splitting of a mixture with liquid and gaseous hydrocarbons in heat exchangers.

Die in der Natur auftretenden Gemische an Kohlenwasserstoffen weisen in der Regel nicht die erwünschten Zusammensetzungen auf, so daß eine rein destillative Aufarbeitung der Erdölprodukte nicht ausreichend ist. Um den Bedürfnissen Rechnung zu tragen, wurden verschiedene Verfahren zur Umwandlung der natürlich vorkommenden Erdölprodukte entwickelt, wobei die Verfahren der thermischen Umwandlung mit und ohne Einsatz von Katalysatoren von besonderer Bedeutung sind. Diese thermischen Umsetzungen erfolgen bei Temperaturen zwischen 600° C und 860° C, je nachdem, welche Ausgangsproduktmischung vorliegt und welche Endproduktmischung erhalten werden soll.The mixtures of hydrocarbons occurring in nature usually do not show the desired Compositions so that a purely distillative Refurbishing petroleum products is not sufficient. Around Different needs were taken into account Process for converting the naturally occurring Petroleum products developed using the process of thermal conversion with and without the use of Catalysts are of particular importance. This thermal reactions take place at temperatures between 600 ° C and 860 ° C, depending on the starting product mixture is present and which end product mixture obtained shall be.

Im Sinne einer möglichst hohen Verwertung werden neben den flüssigen gesättigten und ungesättigten geradkettigen, verzweigtkettigen, zyklischen und aromatischen Kohlenwasserstoffen auch gasförmige Kohlenwasserstoffe eingesetzt. Diese gasförmigen Kohlenwasserstoffe stammen zumeist aus den Aufarbeitungseinrichtungen nach den Spaltanlagen bzw. Produktionsanlagen für die unterschiedlichsten Produktmischungen. Diese gasförmigen Produkte werden in der Regel in die zu der Spaltanlage führenden Zuleitungen für die flüssigen Kohlenwasserstoffe eingeleitet. Dadurch wird einerseits die Einsatzbreite der Anlage wesentlich erhöht und anderseits tritt eine wesentliche Verringerung von Rohrleitungen ein, da parallel geführte Rohrleitungen, u. zw. für die gasförmigen Kohlenwasserstoffe und die flüssigen Kohlenwasserstoffe, vermieden werden können.In order to achieve the highest possible recovery, in addition to the liquid saturated and unsaturated straight-chain, branched chain, cyclic and aromatic hydrocarbons gaseous hydrocarbons are also used. These gaseous hydrocarbons come from mostly from the processing facilities according to Splitting plants or production plants for the most varied Product blends. This gaseous Products are usually delivered to the slitting line leading supply lines for the liquid hydrocarbons initiated. As a result, the range of uses of the Plant significantly increased and on the other hand occurs a substantial reduction in piping since parallel pipelines, u. for the gaseous Hydrocarbons and the liquid hydrocarbons, can be avoided.

Die Kohlenwasserstoffgemische müssen in der Regel in mehreren Stufen bis zur Temperatur der thermischen Spaltung erhitzt werden. Der Durchsatz in den einzelnen Stufen, d. h. den Wärmetauschern, ist in der Regel volumsmäßig, insbesondere in der ersten Stufe, auf Teilverdampfung der flüssigen Kohlenwasserstoffe ausgelegt. Bei einem Überangebot an flüssigen Kohlenwasserstoffen wird ein Teil derselben über eine Umwegleitung von vor dem Eingang in den Wärmetauscher in die Leitung nach dem Wärmetauscher eingeleitet, um eine zu starke Abkühlung, z. B. unterhalb des Taupunktes des Wärmetauschermediums, z. B. Rauchgase, zu vermeiden. Durch diese Umwegleitung kommt es allerdings dazu, daß die zur Vorwärmung bestimmte Produktmischung nicht im erwünschten Umfang erhitzt wird, da ein zu geringer Anteil durch den Wärmetauscher geleitet wird.The hydrocarbon mixtures usually need to be in several stages up to the temperature of the thermal Cleavage to be heated. The throughput in each Stages, d. H. the heat exchangers, is usually by volume, especially in the first stage, on partial evaporation of liquid hydrocarbons. With an oversupply of liquid hydrocarbons a part of it is via a detour from before Entry into the heat exchanger in the line after the Heat exchanger initiated to cool down too much, e.g. B. below the dew point of the heat exchange medium, e.g. B. flue gases to avoid. Through this detour However, it happens that the one intended for preheating Product mixture is not heated to the desired extent, because too little is passed through the heat exchanger becomes.

Die erfindungsgemäße Vorrichtung zum thermischen Spalten eines Gemisches mit flüssigen und gasförmigen Kohlenwasserstoffen, wobei zumindest eine Rohrleitung für das Gemisch in einem Wärmetauscher mündet, welche gegebenenfalls mit einer aus dem Wärmetauscher führenden Rohrleitung über eine Umwegleitung mit einem im Durchfluß regelbaren Absperrorgan fluidleitend verbunden ist, und die aus dem Wärmetauscher führende Rohrleitung, in welche zumindest eine weitere Rohrleitung für überhitzten Wasserdampf mündet, ihrerseits in einen weiteren Wärmetauscher mündet, dessen Ausgangsleitung in einen nachgeschalteten Wärmetauscher, gegebenenfalls mit Katalysator, mündet, dessen Ausgangsleitung in eine Kühlund Auftrenneinrichtung mündet, besteht im wesentlichen darin, daß in Strömungsrichtung gesehen vor dem Wärmetauscher zumindest ein Gasabscheider für die Abtrennung eines gasförmigen Anteiles aus der Mischung vorgesehen ist, wobei die Umwegleitung eine Gasleitung, welche ein im Durchfluß regelbares Absperrorgan aufweist, aus dem Gasabscheider in einen weiteren Wärmetauscher, insbesondere über die weitere Rohrleitung, mündet.The device according to the invention for thermal splitting a mixture of liquid and gaseous hydrocarbons, with at least one pipe for that Mixture opens into a heat exchanger, which if necessary with one leading out of the heat exchanger Pipeline through a detour line with one in flow controllable shut-off device is fluidly connected, and the pipeline leading from the heat exchanger into which at least one more pipe for overheated Water vapor flows into another Heat exchanger opens, the output line in one downstream heat exchanger, if necessary with Catalyst, opens, the outlet line in a cooling and Splitting device opens, essentially exists in that seen in the direction of flow before Heat exchanger at least one gas separator for the Separation of a gaseous fraction from the mixture is provided, the detour line being a gas line, which has a shut-off device which can be regulated in the flow, from the gas separator into another heat exchanger, in particular via the further pipeline.

Dadurch, daß vor dem ersten Wärmetauscher der gasförmige Anteil aus der Ausgangsproduktmischung wieder abgeschieden wird, können doppelte Zuleitungen für die flüssigen bzw. gasförmigen Ausgangsprodukte vermieden werden. Weiters tritt in den Wärmetauscher eine Mischung, welche im wesentlichen gasfrei sein kann, ein, so daß der bevorzugte Wärmeaustausch zu den flüssigen Produkten erfolgen kann, welcher auf Grund der höheren spezifischen Wärme von Flüssigkeiten gegenüber Gasen besonders wirksam erfolgen kann. Das Gas kann vom Gasabscheider über eine Rohrleitung, die entweder in den weiteren Wärmetauscher oder bereits in den eigentlichen Spaltofen mündet, geleitet sein. Die Gasleitung dient somit als Umwegleitung für den ersten Wärmetauscher, womit auch die Temperatur des Wärmetauschermediums, z. B. Rauchgase, gesteuert werden kann. Damit kann einerseits ein besonders hoher Wärmeaustausch erreicht werden, wobei anderseits eine zu große Abkühlung, z. B. der Rauchgase, und damit eine Unterschreitung der Taupunkttemperatur sowie der damit auftretenden Korrosion vermieden werden kann.Characterized in that the gaseous in front of the first heat exchanger Portion separated from the starting product mixture double supply lines for the liquid or gaseous starting products can be avoided. Furthermore a mixture enters the heat exchanger, which can be essentially gas-free, so that the preferred Heat exchange to the liquid products can take place which due to the higher specific heat of Liquids are particularly effective against gases can. The gas can pass through a gas separator Pipeline either in the further heat exchanger or already opens into the actual cracking furnace, be led. The gas line thus serves as a detour line for the first heat exchanger, which also means the temperature the heat exchange medium, e.g. B. flue gases controlled can be. On the one hand, this allows a particularly high Heat exchange can be achieved, on the other hand one too great cooling, e.g. B. the flue gases, and thus one Falling below the dew point temperature and thus occurring corrosion can be avoided.

Ist der Gasabscheider als Schwerkraftabscheider ausgebildet, so kann ohne großen Druckverlust eine einfache Abscheidung der gasförmigen Anteile aus der Gas/Flüssigkeitsmischung erfolgen.If the gas separator is designed as a gravity separator, so can be a simple one without great pressure loss Separation of the gaseous components from the gas / liquid mixture respectively.

Eine besonders wirksame Trennung zwischen Gas und Flüssigkeit kann über einen Zyklon erfolgen.A particularly effective separation between gas and Liquid can be done via a cyclone.

Mündet die Gasleitung aus dem Gasabscheider in Strömungsrichtung gesehen vor der weiteren Leitung für den Wasserdampf in die ausgehende Leitung aus dem Wärmetauscher, so kann bereits in den weiteren Wärmetauscher ein Produktgemisch aus den flüssigen Kohlenwasserstoffen, den gasförmigen Kohlenwasserstoffen und dem Wasserdampf eintreten, so daß der Partialdampferniedrigung in dem Wärmetauscher besonders günstig Rechnung getragen ist, womit die flüssigen Kohlenwasserstoffe besonders schnell verdampfen können und eine weitere hohe Aufnahme von Wärme in diesem Wärmetauscher erreicht wird.If the gas line opens into the gas separator Flow direction seen before the further line for the Water vapor in the outgoing pipe from the heat exchanger, so can already in the further heat exchanger a product mixture of the liquid hydrocarbons, the gaseous hydrocarbons and water vapor occur so that the partial steam lowering in the Heat exchanger is taken into account particularly cheaply, which makes the liquid hydrocarbons particularly quick can evaporate and another high absorption of heat is achieved in this heat exchanger.

Mündet die Gasleitung aus dem Gasabscheider in den nachgeschalteten Wärmetauscher, also in den Spaltofen, insbesondere in die Ausgangsleitung aus dem weiteren Wärmetauscher, so kann bei einem besonders großen Angebot an gasförmigen Produkten im Gemisch auch im weiteren Wärmetauscher ein Wärmeübergang ohne nachteilige Beeinflussung der gasförmigen Ausgangsprodukte erreicht werden.If the gas line flows from the gas separator into the downstream heat exchanger, i.e. in the cracking furnace, especially in the output line from the rest Heat exchanger, so with a particularly large range of gaseous products in the mixture also in the further Heat exchanger a heat transfer without disadvantageous Influencing the gaseous starting products achieved will.

Mündet die Gasleitung aus dem Gasabscheider in die weitere Rohrleitung für den Wasserdampf, so kann eine Mischung von Wasserdampf und gasförmigen Produkten erreicht werden, die ihrerseits sodann in die Zuleitung für den weiteren Wärmetauscher eingeleitet werden kann.The gas line flows from the gas separator into the other Pipe for the water vapor, so a mixture of Water vapor and gaseous products can be achieved in turn then into the supply line for the further Heat exchanger can be initiated.

Mündet die Gasleitung aus dem Gasabscheider in einen Dampfüberhitzer, so kann das Gas zusammen mit dem Wasserdampf erhitzt werden.The gas line flows out of the gas separator into one Steam superheater, so the gas along with the water vapor be heated.

Ist eine zusätzliche Umwegleitung zum Wärmetauscher, insbesondere mit einem im Durchfluß regelbaren Absperrorgan, vorgesehen, welche von der Rohrleitung nach dem Gasabscheider, die in den Wärmetauscher mündet, abzweigt, und vorzugsweise in die weitere Rohrleitung nach der Einmündung der Gasrohrleitung einmündet, so können auch stoßförmige Überangebote von flüssigen Kohlenwasserstoffen ohne druckmäßige Überbelastung des Wärmetauschers abgefangen und gegebenenfalls gesteuert werden.Is an additional detour line to the heat exchanger, in particular with a shut-off device which can be regulated in the flow, provided by the pipeline after the Gas separator, which opens into the heat exchanger, branches off, and preferably in the further pipeline after the Confluence of the gas pipeline, so can also bursty oversupply of liquid hydrocarbons without pressure overload of the heat exchanger intercepted and controlled if necessary.

Wärmetauscher können auch als Gruppen von Wärmetauschern aufgebaut sein.Heat exchangers can also be used as groups of heat exchangers be constructed.

Im folgenden wird die Erfindung anhand der Zeichnungen und Beispiele näher erläutert.In the following the invention with reference to the drawings and Examples explained in more detail.

Es zeigen:

  • Fig. 1 in schematischer Darstellung einen Spaltofen mit zwei vorgeschalteten Wärmetauschern und
  • Fig. 2 und 3 in schematischer Darstellung Gasabscheider.
    • Show it:
  • Fig. 1 shows a schematic representation of a cracking furnace with two upstream heat exchangers and
  • 2 and 3 in a schematic representation gas separator.

    • Bei dem in Fig. 1 dargestellten Schemata einer Olefinerzeugungsanlage vereinigen sich die Rohrleitungen R1 und R2, die flüssige Kohlenwasserstoffe (Benzin) bzw. gasförmige Kohlenwasserstoffe mit zwei bis vier Kohlenstoffatomen leiten zur Rohrleitung R3, die ihrerseits in den Gasabscheider G mündet. Die flüssigen Produkte werden sodann über die Rohrleitung R3 in den Wärmetauscher W1 geleitet. Die gasförmigen Produkte aus dem Gasabscheider G gelangen über die Gasleitung G1, die als Umwegleitung für den Wärmetauscher W1 dient, in die aus dem Wärmetauscher W1 führende Rohrleitung R4. In diese Rohrleitung R4 mündet auch eine Dampfleitung D1, die den Dampf aus dem Dampfüberhitzer D weiterleitet. Der weitere Wärmetauscher W2, in welchen die Rohrleitung R4 mündet, ist über eine Ausgangsleitung R5 mit dem Spaltofen, dem nachgeschalteten Wärmetauscher S, verbunden. Aus dem Wärmetauscher S führt eine Rohrleitung R6 in eine Kühl- und Auftrennungseinrichtung K+A. Der Dampfüberhitzer D, in welchem gegebenenfalls Dampf erzeugt wird, der Spaltofen, der Wärmetauscher S sowie die Wärmetauscher W1 und W2 sind als Rohrbündelwärmetauscher ausgebildet, wobei als Wärmeträgermedium Rauchgas dient. In der Gasleitung G1 kann ein im Durchfluß regelbares Ventil V1 vorgesehen sein, das dann geschlossen wird, wenn es erwünscht ist, daß das gesamte Produktgemisch durch die Rohrleitung R3 in den Wärmetauscher W1 geleitet wird. Eine Gasleitung G2 kann auch in die Ausgangsleitung R5 des Wärmetauschers W2 führen, oder auch wie die Gasleitung G3 direkt in den Spaltofen, den Wärmetauscher S einmünden. Diese Gasleitungen können im Durchfluß regelbare Ventile V2 und V3 aufweisen.In the diagram of an olefin production plant shown in FIG. 1, the pipes R 1 and R 2 , which conduct liquid hydrocarbons (gasoline) or gaseous hydrocarbons with two to four carbon atoms, lead to the pipe R 3 , which in turn opens into the gas separator G. The liquid products are then passed through the pipe R 3 into the heat exchanger W 1 . The gaseous products from the gas separator G pass through the gas line G 1 , which serves as a detour line for the heat exchanger W 1 , into the pipeline R 4 leading from the heat exchanger W 1 . A steam line D 1 , which forwards the steam from the steam superheater D, also opens into this pipeline R 4 . The further heat exchanger W 2 , in which the pipeline R 4 opens, is connected via an output line R 5 to the cracking furnace, the downstream heat exchanger S. A pipe R 6 leads from the heat exchanger S into a cooling and separation device K + A. The steam superheater D, in which steam is optionally generated, the cracking furnace, the heat exchanger S and the heat exchangers W 1 and W 2 are designed as shell-and-tube heat exchangers, with flue gas serving as the heat transfer medium. A valve V 1 which can be regulated in the flow can be provided in the gas line G 1 and is closed when it is desired that the entire product mixture is passed through the pipe R 3 into the heat exchanger W 1 . A gas line G 2 can also lead into the outlet line R 5 of the heat exchanger W 2 , or, like the gas line G 3, also lead directly into the cracking furnace, the heat exchanger S. These gas lines can have valves V 2 and V 3 which can be regulated in the flow.

    Ist es erwünscht, daß das Gas noch erhitzt wird, kann es über eine Leitung G4 dem Dampfüberhitzer D oder gegebenenfalls einem Dampferzeuger zugeführt werden.If it is desired that the gas is still heated, it can be fed via a line G 4 to the steam superheater D or, if appropriate, to a steam generator.

    Zusätzlich zu der bzw. den Gasleitung(en) G1 bis G4 kann auch eine weitere Umwegleitung U1 vorgesehen sein, die von der Rohrleitung R3 vor dem Wärmetauscher W1 abzweigt und in die Rohrleitung R4 nach dem Wärmetauscher W1 einmündet. Diese Umwegleitung U1 weist ein im Durchfluß regelbares Ventil V4 auf. In addition to the gas line (s) G 1 to G 4 , a further detour line U 1 can also be provided, which branches off from the pipe line R 3 in front of the heat exchanger W 1 and opens into the pipe line R 4 after the heat exchanger W 1 . This detour line U 1 has a flow controllable valve V 4 .

    Die Wärmetauscher W1 und W2 sowie der Dampfüberhitzer D und der Spaltofen, der Wärmetauscher S werden nacheinander von Rauchgasen, die als Wärmetauschermedium dienen, durchströmt. Die Rauchgase treten entsprechend dem Pfeil X1 durch den Spaltofen, den Wärmetauscher S, anschließend in einen nicht dargestellten Hochdruckdampfüberhitzer, in welchem Hochdruckdampf erzeugt werden kann, welcher nicht dem Prozeß zugeführt werden muß. Sodann tritt das Rauchgas entsprechend dem Pfeil X3 in den Dampfüberhitzer D, in welchen entsprechend dem Pfeil Z Prozeßdampf eingeleitet wird. Aus dem Dampfüberhitzer D tritt das Rauchgas entsprechend dem Pfeil X4 in den Wärmetauscher W2, aus welchem derselbe in einen nicht dargestellten Kesselspeisewasservorwärmer eintreten kann, welcher ebenfalls nicht im Rahmen des erfindungsgemäßen Verfahrens benötigt wird. Aus dieser Vorwärmung tritt das Rauchgas gemäß Pfeil X6 in den Wärmetauscher W1 ein, aus welchem sodann die Rauchgase gemäß Pfeil X7 dem Kamin zugeleitet werden. Die Anordnung der Wärmetauscher ist entsprechend dem erforderlichen Wärmepotential durchgeführt, wobei der Spaltofen, der Wärmetauscher S die höchste Temperatur der Rauchgase erfordert, wohingegen der Wärmetauscher W1 Rauchgase mit einer wesentlich niedrigeren Temperatur erfordert.The heat exchangers W 1 and W 2 as well as the steam superheater D and the cracking furnace, the heat exchanger S are successively flowed through by flue gases, which serve as heat exchange medium. The flue gases pass according to arrow X 1 through the cracking furnace, the heat exchanger S, then into a high-pressure steam superheater, not shown, in which high-pressure steam can be generated, which does not have to be fed to the process. The flue gas then enters the steam superheater D according to the arrow X 3, in which process steam is introduced according to the arrow Z. From the steam superheater D, the flue gas enters according to the arrow X 4 into the heat exchanger W 2 , from which it can enter a boiler feed water preheater, not shown, which is also not required in the process according to the invention. From this preheating, the flue gas enters the heat exchanger W 1 according to arrow X 6 , from which the flue gases are then fed to the chimney according to arrow X 7 . The arrangement of the heat exchangers is carried out in accordance with the required heat potential, the cracking furnace, the heat exchanger S requiring the highest temperature of the flue gases, whereas the heat exchanger W 1 requires flue gases with a much lower temperature.

    Der in Fig. 2 schematisch dargestellte Gasabscheider G weist ein zylinderisches Rohr 1 auf, das als äußerer Behälter dient. In diesen äußeren Behälter mündet die Rohrleitung R3, über welche das Produktgemisch flüssig und gasförmig eingebracht wird. Im zylindrischen Rohr 1 erfolgt eine extreme Verlangsamung der Strömungsgeschwindigkeit, wobei gleichzeitig eine Trennung der gasförmigen und der flüssigen Phase eintritt. Die flüssige Phase wird über die austretende Rohrleitung R3 abgeleitet, wohingegen die gasförmige Phase über das zylindrische Rohr 2, das sich in die Gasleitung G1 fortsetzt, abgeführt wird und so in die Rohrleitung R4 bei offenem Ventil V1 gelangt.The gas separator G shown schematically in FIG. 2 has a cylindrical tube 1 which serves as an outer container. The pipeline R 3 , into which the product mixture is introduced in liquid and gaseous form, opens into this outer container. In the cylindrical tube 1 there is an extreme slowdown in the flow velocity, at the same time a separation of the gaseous and the liquid phase occurs. The liquid phase is discharged via the exiting pipeline R 3 , whereas the gaseous phase is discharged via the cylindrical pipe 2, which continues into the gas line G 1 , and thus reaches the pipeline R 4 with the valve V 1 open.

    Bei dem in Fig. 3 dargestellten Gasabscheider liegt ein Zyklon vor, wobei die Rohrleitung R3 tangential in den kegelförmigen Behälter 3 mündet. Das Produktgemisch bewegt sich spiralförmig entlang der äußeren Behälterwandung nach unten und trennt sich hiebei auf. Die flüssige Phase wird über die am Boden befindliche Rohrleitung R3 abgezogen, wohingegen die gasförmige Phase über die Gasleitung G1 zum Abzug gelangt.In the gas separator shown in FIG. 3 there is a cyclone, the pipe R 3 opening tangentially into the conical container 3. The product mixture moves downwards in a spiral along the outer container wall and separates. The liquid phase is withdrawn via the pipeline R 3 located on the bottom, whereas the gaseous phase is withdrawn via the gas line G 1 .

    Beispiel 1:Example 1:

    Über die Rohrleitung R3 mit einer Nennweite von 80 mm wurde 1.625 kg flüssiges Benzin pro Stunde und 750 kg gasförmige Kohlenwasserstoffe mit 2 bis 4 Kohlenstoffatomen pro Stunde in den Wärmetauscher W1 geleitet. Es war eine Umwegleitung U1 vorgesehen. Das in den Wärmetauscher W1 eintretende Produktgemisch wies eine Temperatur von 60° C auf. Beim Austritt trat eine Erwärmung auf 250° C auf. 75 Vol.-% der flüssigen und 15 Vol.-% der gasförmigen Phase des Produktes wurden durch die Umwegleitung U1 geleitet, welche somit nicht erwärmt wurden. Das Produktgemisch gelangte sodann über die Rohrleitung R4 mit Nennweite 80 mm, in welche 1.400 kg/h Wasserdampf mit einer Temperatur von 491° C eingeleitet wurde, in den Wärmetauscher W2. Das eintretende Produktgemisch wurde im Wärmetauscher W2 auf 440° C erhitzt. Das so erhitzte Produktgemisch ist sodann über die Rohrleitung R5 mit Nennweite 80 mm in den Spaltofen S geleitet. Der Spaltofen ist als Wärmetauscher ausgebildet, in welchem die Mischung weiter erhitzt wurde. Aus der Rohrleitung R6 trat ein Gemisch mit 855° C aus.1,625 kg of liquid petrol per hour and 750 kg of gaseous hydrocarbons with 2 to 4 carbon atoms per hour were fed into the heat exchanger W 1 via the pipeline R 3 with a nominal diameter of 80 mm. A detour line U 1 was provided. The product mixture entering the heat exchanger W 1 had a temperature of 60 ° C. A warming to 250 ° C. occurred at the outlet. 75 vol .-% of the liquid and 15 vol .-% of the gaseous phase of the product were passed through the detour U 1 , which were therefore not heated. The product mixture then entered the heat exchanger W 2 via the R 4 pipeline with a nominal diameter of 80 mm, into which 1,400 kg / h of steam at a temperature of 491 ° C. was introduced. The incoming product mixture was heated to 440 ° C in the heat exchanger W 2 . The product mixture heated in this way is then passed through the pipe R 5 with a nominal diameter of 80 mm into the cracking furnace S. The cracking furnace is designed as a heat exchanger in which the mixture has been heated further. A mixture at 855 ° C. emerged from the pipeline R 6 .

    Beispiel 2:Example 2:

    Über die Rohrleitung R3 mit einer Nennweite von 80 mm gelangte eine Produktmischung aus 1.750 kg/h, flüssig, 750 kg/h, gasförmig, in den Wärmetauscher W1. Es war hiebei ein Gasabscheider mit Gasleitung G1 vorgesehen. Das in den Wärmetauscher W1 eintretende Produktgemisch wies eine Temperatur von 60° C auf. Beim Austritt trat eine Erwärmung auf 220° C auf. 15 Vol.-% der gasförmigen Phase und kein Anteil der flüssigen Phase des Produktes wurden durch die Gasleitung G1 geleitet, die somit nicht erwärmt wurde. Das Produktgemisch gelangte sodann über die Rohrleitung R4, in welche Wasserdampf mit 483° C und in einer Menge von 1.300 kg/h eingeleitet wurde mit Nennweite 80 mm in den Wärmetauscher W2. Das eintretende Produktgemisch wurde im Wärmetauscher W2 auf 450° C erhitzt. Das so erhitzte Produktgemisch wurde sodann über die Rohrleitung R5 mit Nennweite 80 mm in den Spaltofen S geleitet. Im Spaltofen selbst wurde auch noch erhitzt. Aus der Rohrleitung R6 trat ein Gemisch mit 855° C aus.A product mixture of 1,750 kg / h, liquid, 750 kg / h, gaseous, entered the heat exchanger W 1 via the pipe R 3 with a nominal width of 80 mm. A gas separator with a gas line G 1 was provided. The product mixture entering the heat exchanger W 1 had a temperature of 60 ° C. Upon exiting, heating to 220 ° C occurred. 15 vol .-% of the gaseous phase and no portion of the liquid phase of the product were passed through the gas line G 1 , which was therefore not heated. The product mixture then reached the pipeline R 4 , into which water vapor at 483 ° C. and in an amount of 1,300 kg / h with a nominal width of 80 mm was introduced into the heat exchanger W 2 . The incoming product mixture was heated to 450 ° C in the heat exchanger W 2 . The product mixture heated in this way was then fed into the cracking furnace S via the pipeline R 5 with a nominal diameter of 80 mm. Heating was also carried out in the cracking furnace itself. A mixture at 855 ° C. emerged from the pipeline R 6 .

    Wie der Vergleich der Beispiele 1 und 2 zeigt, kann mit der Gasabscheidung vor dem Wärmetauscher W1 eine wesentlich bessere Erhitzung der zum Spaltofen zuzuleitenden Mischung erreicht werden, und weiters eine wesentliche Abkühlung des Wärmetauschermediums beim Austritt aus dem Wärmetauscher W1 erreicht werden, so daß die Wirkung des Spaltofens bei gleichbleibendem Energieeinsatz wesentlich erhöht werden kann.As the comparison of Examples 1 and 2 shows, with the gas separation before the heat exchanger W 1, a significantly better heating of the mixture to be fed to the cracking furnace can be achieved, and furthermore a substantial cooling of the heat exchange medium when it exits the heat exchanger W 1 can be achieved, so that the effect of the cracking furnace can be increased significantly while using the same amount of energy.

    Claims (8)

    1. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons, whereby at least one pipeline (R3) for the mixture debouches into a heat exchanger (W1) and if necessary is connected in a fluid-conducting manner with a pipeline (R4) leading out of the heat exchanger by means of a bypass line with a shut-off device (V1) of controllable throughput, and the pipeline (R4) leading out of the heat exchanger (W1) and into which at least one further pipeline (D1) for superheated water vapour debouches, for its part debouches into a further heat exchanger (W2) whose output line (R5) debouches into a following heat exchanger (S), if necessary with a catalyst, whose output line (R6) debouches into a cooling and separating device (K+A), characterised in that at least one gas separator for separating a gaseous proportion from the mixture is provided before the heat exchanger (W1) viewed in the direction of flow, whereby the bypass line, a gas line (G1) which exhibits a shut-off device (V1) of controllable throughput, out of the gas separator (G) debouches into a further heat exchanger (W2, S, D), in particular through the further pipeline (R4).
    2. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to claim 1, characterised in that the gas separator (G) takes the form of a gravity separator.
    3. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to claim 1, characterised in that the gas separator (G) takes the form of a cyclone.
    4. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to one of claims 1, 2 or 3, characterised in that the gas line (G1) out of the gas separator (G) before the further line (D1) for water vapour viewed in the direction of flow, debouches into the line (R4) leading out of the heat exchanger (W1).
    5. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to one of claims 1 to 4, characterised in that the gas line (G2) out of the gas separator (G) debouches into the following heat exchanger (S), in particular into the output line (R5) out of the further heat exchanger (W2).
    6. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to one of claims 1 to 5, characterised in that the gas line (G2) out of the gas separator debouches into the further pipeline (D1).
    7. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to one of claims 1 to 6, characterised in that the gas line (G4) out of the gas separator (G) debouches into a vapour superheater (D).
    8. Device for thermal cracking of a mixture with liquid and gaseous hydrocarbons according to one of claims 1 to 6, characterised in that an additional bypass line (U1) bypassing the heat exchanger (W1) is provided which branches off the pipeline (R3) following the gas separator (G) and debouching into the heat exchanger (W1), and preferably debouches into the further pipeline (R4) after the connection of the gas line (G1).
    EP94890007A 1993-01-27 1994-01-14 Apparatus for the thermal cracking of a mixture of liquid and gaseous hydrocarbons Expired - Lifetime EP0609191B1 (en)

    Applications Claiming Priority (2)

    Application Number Priority Date Filing Date Title
    AT0013793A AT398428B (en) 1993-01-27 1993-01-27 DEVICE FOR THERMALLY CLEAVING A MIXTURE WITH LIQUID AND GASEOUS HYDROCARBONS
    AT137/93 1993-01-27

    Publications (2)

    Publication Number Publication Date
    EP0609191A1 EP0609191A1 (en) 1994-08-03
    EP0609191B1 true EP0609191B1 (en) 1998-07-29

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    EP94890007A Expired - Lifetime EP0609191B1 (en) 1993-01-27 1994-01-14 Apparatus for the thermal cracking of a mixture of liquid and gaseous hydrocarbons

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    EP (1) EP0609191B1 (en)
    AT (1) AT398428B (en)
    CZ (1) CZ283129B6 (en)
    DE (1) DE59406524D1 (en)
    DK (1) DK0609191T3 (en)
    ES (1) ES2121177T3 (en)
    FI (1) FI115466B (en)
    HU (1) HU214480B (en)
    NO (1) NO306681B1 (en)
    SI (1) SI9400032A (en)
    SK (1) SK279373B6 (en)

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    * Cited by examiner, † Cited by third party
    Publication number Priority date Publication date Assignee Title
    EP4259751A1 (en) 2020-12-10 2023-10-18 TotalEnergies OneTech Belgium Method for improving feedstock flexibility of steam cracking
    EP4074809A1 (en) 2021-04-14 2022-10-19 Total Research & Technology Feluy Process and apparatus for cracking of thermally unstable feedstock

    Family Cites Families (3)

    * Cited by examiner, † Cited by third party
    Publication number Priority date Publication date Assignee Title
    US4479869A (en) * 1983-12-14 1984-10-30 The M. W. Kellogg Company Flexible feed pyrolysis process
    JPH0819420B2 (en) * 1988-09-05 1996-02-28 三井石油化学工業株式会社 Degradation method for low-grade raw materials
    DE4105095A1 (en) * 1991-02-19 1992-08-20 Linde Ag METHOD FOR CONTROLLING PROCESSES IN SPLITTING OVENS FOR OLEFIN PRODUCTION

    Also Published As

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    HU214480B (en) 1998-03-30
    NO940252L (en) 1994-07-28
    EP0609191A1 (en) 1994-08-03
    NO940252D0 (en) 1994-01-25
    AT398428B (en) 1994-12-27
    DE59406524D1 (en) 1998-09-03
    HUT69458A (en) 1995-09-28
    FI115466B (en) 2005-05-13
    CZ283129B6 (en) 1998-01-14
    NO306681B1 (en) 1999-12-06
    CZ17394A3 (en) 1994-08-17
    SI9400032A (en) 1994-09-30
    DK0609191T3 (en) 1999-04-26
    FI940385A0 (en) 1994-01-26
    ES2121177T3 (en) 1998-11-16
    ATA13793A (en) 1994-04-15
    FI940385A (en) 1994-07-28
    HU9400231D0 (en) 1994-05-30
    SK8194A3 (en) 1994-11-09
    SK279373B6 (en) 1998-10-07

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