EP1285903A1 - Process for the preparation of paraffines from educts containing cyclic hydrocarbons - Google Patents

Process for the preparation of paraffines from educts containing cyclic hydrocarbons Download PDF

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EP1285903A1
EP1285903A1 EP02018081A EP02018081A EP1285903A1 EP 1285903 A1 EP1285903 A1 EP 1285903A1 EP 02018081 A EP02018081 A EP 02018081A EP 02018081 A EP02018081 A EP 02018081A EP 1285903 A1 EP1285903 A1 EP 1285903A1
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Prior art keywords
reaction
reactor
aromatics
carried out
cyclic hydrocarbons
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German (de)
French (fr)
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EP1285903B1 (en
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Helmut Fritz
Ulrike Dr. Wenning
Heinz BÖLT
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Linde GmbH
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Linde GmbH
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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Definitions

  • the invention relates to a method for producing paraffins from cyclic Feedstocks containing hydrocarbons such as mineral oil fractions and / or Fractions from thermal or catalytic conversion plants containing alkanes, Alkenes, cyclic alkanes and / or aromatics by reaction with a zeolite catalyst.
  • hydrocarbons such as mineral oil fractions and / or Fractions from thermal or catalytic conversion plants containing alkanes, Alkenes, cyclic alkanes and / or aromatics
  • the present invention has for its object a method of the beginning mentioned type so that high yields in an economical manner can be achieved.
  • This object is achieved in that the implementation under Isothermal conditions is carried out in a cooled reactor.
  • the conversion of the starting materials into externally cooled Tubes of the reactor performed.
  • Heat transfer media are particularly suitable for melts and heat transfer oils.
  • the cyclic hydrocarbon feedstocks are advantageously used hydrogenated in a pretreatment stage to a feed stream that predominantly Contains naphthenes and up to 40 vol.% Aromatics.
  • a nickel catalyst is expediently used for hydrogenation. From procedural For reasons, it can be advantageous to reduce the aromatic content in the feed stream to below 5 % By volume, preferably at most 2% by volume.
  • the cooled reactor is one adiabatic catalyst bed with a hydrogenation catalyst immediately upstream, where by hydrogenation of hydrocarbons resulting waste heat further preheating of the feed materials for the subsequent isothermal reaction is used.
  • the use of external energy for Heating of the feed materials to those necessary for the isothermal reaction Reaction temperature can be minimized, and there is no need for an oven.
  • the pretreatment stage shown in Figure 1 is used to hydrogenate the cyclic Feedstocks containing hydrocarbons.
  • a stream of C5 + Hydrocarbons from an olefin plant undergo selective hydrogenation and Desulfurization and fractionation 1 fed.
  • the pyrolysis heavy gasoline obtained with predominantly C7 + hydrocarbons has an aromatic content from typically 60 to 90% by volume, in the present example 87% by volume.
  • a pump 2 turns the pyrolysis heavy gasoline to a pressure of approx. 30 bar compressed and divided into two partial streams 3 and 4.
  • the partial stream 4 is a Heat exchanger 5 heated and one with a temperature of 80 to 120 ° C.
  • Hydrogenation stage 6 with three catalyst beds which contain a nickel catalyst, given up.
  • the other partial stream 3 is distributed to the hydrogenation stage 6.
  • the aromatics are hydrogenated to naphthenes.
  • the product obtained which can contain up to 40 vol.% aromatics, but smaller in the present example 0.5 vol.% Aromatics, is at a temperature of 120 to 160 ° C by means of Line 7 withdrawn, cooled in the heat exchangers 5 and 8, the Heat exchanger 8 is operated with cooling water, and finally one Gas-liquid separation 9 supplied. Liquid product is partly via line 10 recycled and serves to dilute the feedstock for hydrogenation stage 6.
  • the resulting hydrogen gas is in a pressure swing adsorption system (PSA) 11 hydrogen produced were added.
  • PSA pressure swing adsorption system
  • the product stream containing the naphthenes is by means of a Pump 13 to about 25 to 70 bar, preferably 50 to 60 bar, in the present example compressed about 60 bar, preheated by means of heat exchangers 14 and 15 and one Heating level 16 supplied.
  • the feed materials heated to approx. 380 ° C are used in the Isothermal reactor 17 initiated.
  • the Isothermal reactor 17 designed as a straight tube reactor.
  • the arranged in the reactor 17 Pipes are cooled from the outside with a heat transfer oil, which is in line 18 circulated.
  • the heat of reaction occurring in the reactor 17 is by means of Heat transfer oil discharged to an external steam generator 19.
  • the isothermal reactor 17 contains a zeolite catalyst.
  • the naphthenes are placed in the reactor isothermal conditions with a constant high conversion rate to paraffins implemented.
  • the reaction products are discharged via line 20 and by means of Heat exchangers 15 and 14 cooled. At one above the dew point Temperature of 144 ° C, the reaction products to that shown in Figure 3 Submit post processing level.
  • the reaction products fractionated.
  • the reaction products are passed to a scrubber 22 via line 21 fed.
  • the gaseous product is discharged from the head of the scrubber 22 via line 23 dissipated, cooled in a heat exchanger 24 against cooling water and a gas-liquid separation 25 fed.
  • the gaseous product obtained is about Line 26 fed to a further gas-liquid separation stage 27. That in this Separation stage resulting gaseous product is at a temperature of approx. 15 ° C passed through a dryer 28 to a plate heat exchanger 29.
  • gaseous hydrogen is separated and by means of Line 31 fed into the process.
  • the liquid obtained in the separation stage 30 The product is finally discharged from the aftertreatment stage via line 32 and stands as a feed with a very high paraffin content for the steam cracker Olefin plant available.
  • the condensate obtained in the scrubber 22 contains partially propane, and is via line 33 of a propane stripping in a Stripping column 34 fed. Aromatics that are produced in the process are finally added a return line 35 to the pretreatment stage shown in FIG. 1 recycled.
  • FIG. 4 shows the product composition of the product leaving the plant Product stream specified as the insert for the steam cracker of the olefin plant is used (SC feedstock).

Abstract

Production of paraffins comprises reaction of feed containing cyclic hydrocarbons on a zeolite catalyst under isothermal conditions in a cooled reactor.

Description

Die Erfindung betrifft ein Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen wie Mineralölfraktionen und/oder Fraktionen aus thermischen oder katalytischen Konversionsanlagen enthaltend Alkane, Alkene, zyklische Alkane und/oder Aromaten durch Umsetzen mit einem Zeolith-Katalysator.The invention relates to a method for producing paraffins from cyclic Feedstocks containing hydrocarbons such as mineral oil fractions and / or Fractions from thermal or catalytic conversion plants containing alkanes, Alkenes, cyclic alkanes and / or aromatics by reaction with a zeolite catalyst.

Aus Umweltschutzgründen wird eine Verringerung des Aromatengehalts in Kraftstoffen angestrebt. Daher müssen in Zukunft aromatenreiche Fraktionen, die bisher den Kraftstoffen zur Erhöhung der Oktanzahlen zugesetzt wurden, einer neuen Verwendung zugeführt werden. Dies trifft auch für das bei der Erzeugung von Ethylen und Propylen in Olefinanlagen anfallende aromatenreiche Pyrolyse-Schwerbenzin zu. In der DE 199 49 211 A1 wird hierzu vorgeschlagen, solche Fraktionen mittels eines Zeolith-Katalysators zu n-Alkanen, insbesondere Ethan, Propan und n-Butan, umzusetzen. Diese Stoffe können schließlich wieder dem Einsatz der Olefinanlage zugemischt werden.For environmental reasons, a reduction in the aromatic content in fuels sought. For this reason, fractions rich in aromatics, which previously A new fuel was added to increase octane numbers Use are fed. This also applies to the production of ethylene and propylene in aromatic pyrolysis heavy gasoline obtained in olefin plants. DE 199 49 211 A1 proposes such fractions by means of a Zeolite catalyst to n-alkanes, in particular ethane, propane and n-butane, implement. These substances can eventually use the olefin plant again be added.

Der vorliegenden Erfindung liegt die Aufgabe zugrunde, ein Verfahren der eingangs genannten Art so auszugestalten, dass auf wirtschaftliche Weise hohe Ausbeuten erzielt werden können.The present invention has for its object a method of the beginning mentioned type so that high yields in an economical manner can be achieved.

Diese Aufgabe wird erfindungsgemäß dadurch gelöst, dass die Umsetzung unter isothermen Bedingungen in einem gekühlten Reaktor durchgeführt wird.This object is achieved in that the implementation under Isothermal conditions is carried out in a cooled reactor.

Durch Einhaltung von isothermen Bedingungen wird der Tatsache Rechnung getragen, dass der Temperaturunterschied zwischen einer für ausreichende katalytische Aktivität erforderlichen Minimaltemperatur (z. B. 340°C) und einer zur Gewährleistung einer wirtschaftlichen Selektivität zulässigen Maximaltemperatur (410°C) in Relation zu einer adiabaten Temperaturerhöhung von z. B. 325°C sehr gering ist. Unter isothermen Bedingungen ist im Zusammenhang mit der vorliegenden Erfindung zu verstehen, dass die Temperaturerhöhung in der geschlossenen katalytischen Zone auf Werte begrenzt wird, die erheblich unter der entsprechenden adiabaten Temperaturerhöhung und deutlich innerhalb des genannten Betriebsfensters liegen, d. h. z. B. auf 40°C geregelt werden.The fact is taken into account by observing isothermal conditions worn that the temperature difference between one for sufficient Minimum temperature required for catalytic activity (e.g. 340 ° C) and one for Ensuring an economic selectivity permissible maximum temperature (410 ° C) in relation to an adiabatic temperature increase of e.g. B. 325 ° C very is low. Under isothermal conditions is related to the present Invention to understand that the temperature increase in the closed catalytic zone is limited to values significantly below the corresponding adiabatic temperature increase and clearly within the stated Operating window, d. H. z. B. can be regulated to 40 ° C.

Bei der isothermen katalytischen Umwandlung, d.h. bei Reaktionen wie Ringöffnen und -Cracken, anfallende Wärme wird auf hohem Temperatumiveau abgeführt und kann einer sinnvollen Nutzung zugeführt werden. Im Gegensatz dazu wäre bei einer adiabatischen Umsetzung und Kühlung durch Flüssigkeitseinspritzung der Reaktionsprodukte keine sinnvolle Abwärmenutzung möglich. Darüber hinaus bietet die isotherme Verfahrensweise regelungstechnische und ökonomische Vorteile. Eine nachfolgende Trennung der Reaktionsprodukte wird erheblich erleichtert. Durch die erfindungsgemäße Temperaturkontrolle wird eine Optimierung der Selektivität ermöglicht.In isothermal catalytic conversion, i.e. in reactions such as ring opening and -Cracking, heat is dissipated at a high temperature level and can be put to sensible use. In contrast, one would adiabatic conversion and cooling by liquid injection of the Reaction products no sensible use of waste heat possible. It also offers the isothermal procedure control engineering and economic advantages. A subsequent separation of the reaction products is made considerably easier. Through the Temperature control according to the invention is an optimization of the selectivity allows.

Zweckmäßigerweise wird die Umsetzung der Einsatzstoffe in von außen gekühlten Rohren des Reaktors durchgeführt. Hierzu werden die Einsatzstoffe durch die Rohre hindurchgeleitet, während der Rohrmantel mittels eines Wärmeträgers gekühlt wird. Als Wärmeträger eignen sich insbesondere Schmelzen und Wärmeträgeröle.Conveniently, the conversion of the starting materials into externally cooled Tubes of the reactor performed. For this purpose, the feed materials through the pipes passed through, while the tube jacket is cooled by means of a heat transfer medium. As Heat transfer media are particularly suitable for melts and heat transfer oils.

Gemäß einer besonders bevorzugten Ausführungsform der Erfindung wird die Umsetzung der Einsatzstoffe in einem Reaktor mit gewickelten Rohren durchgeführt. Ein solcher Reaktor ist beispielsweise in der DE 34 12 482 A1 beschrieben.According to a particularly preferred embodiment of the invention, the Implementation of the feedstocks carried out in a reactor with coiled tubes. Such a reactor is described for example in DE 34 12 482 A1.

Vorteilhafterweise werden die zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffe in einer Vorbehandlungsstufe zu einem Einsatzstrom hydriert, der überwiegend Naphthene und bis zu 40 Vol.% Aromaten enthält. Zur Hydrierung wird zweckmäßigerweise ein Nickel-Katalysator eingesetzt. Aus verfahrenstechnischen Gründen kann es von Vorteil sein, den Aromatenanteil im Einsatzstrom auf unter 5 Vol.%, vorzugsweise höchstens 2 Vol.%, zu senken.The cyclic hydrocarbon feedstocks are advantageously used hydrogenated in a pretreatment stage to a feed stream that predominantly Contains naphthenes and up to 40 vol.% Aromatics. For hydrogenation a nickel catalyst is expediently used. From procedural For reasons, it can be advantageous to reduce the aromatic content in the feed stream to below 5 % By volume, preferably at most 2% by volume.

Gemäß einer Weiterbildung des Erfindungsgedankens ist dem gekühlten Reaktor ein adiabatisches Katalysatorbett mit einem Hydrierkatalysator unmittelbar vorgeschaltet, wobei durch Hydrierung von Kohlenwasserstoffen anfallende Reaktionsabwärme zur weiteren Vorheizung der Einsatzstoffe für die anschließende isotherme Reaktion eingesetzt wird. Auf diese Weise kann die Verwendung von Fremdenergie zur Aufheizung der Einsatzstoffe auf die für die Isothermreaktion notwendige Reaktionstemperatur minimiert werden, und es kann auf einen Ofen verzichtet werden.According to a development of the inventive concept, the cooled reactor is one adiabatic catalyst bed with a hydrogenation catalyst immediately upstream, where by hydrogenation of hydrocarbons resulting waste heat further preheating of the feed materials for the subsequent isothermal reaction is used. In this way, the use of external energy for Heating of the feed materials to those necessary for the isothermal reaction Reaction temperature can be minimized, and there is no need for an oven.

Im Folgenden soll die Erfindung anhand eines in den Figuren schematisch dargestellten Ausführungsbeispiels näher erläutert werden:In the following, the invention is to be illustrated schematically using one of the figures illustrated embodiment are explained in more detail:

Es zeigen

Figur 1
ein Fließschema der Vorbehandlungsstufe
Figur 2
ein Fließschema der isothermen katalytischen Umsetzung
Figur 3
ein Fließschema der Nachbearbeitungsstufe.
Figur 4
eine Auflistung der Produktbestandteile
Show it
Figure 1
a flow chart of the pre-treatment stage
Figure 2
a flow diagram of the isothermal catalytic conversion
Figure 3
a flow chart of the post-processing stage.
Figure 4
a list of the product components

Die in Figur 1 dargestellte Vorbehandlungsstufe dient zur Hydrierung der die zyklischen Kohlenwasserstoffe enthaltenden Einsatzstoffe. Ein Strom aus C5+ Kohlenwasserstoffen aus einer Olefinanlage wird einer selektiven Hydrierung und Entschwefelung sowie Fraktionierung 1 zugeführt. Das erhaltene Pyrolyse-Schwerbenzin mit überwiegend C7+ Kohlenwasserstoffen weist einen Aromatengehalt von typischerweise 60 bis 90 Vol.%, im vorliegenden Beispiel 87 Vol.% auf. Mittels einer Pumpe 2 wird das Pyrolyse-Schwerbenzin auf einen Druck von ca. 30 bar verdichtet und auf zwei Teilströme 3 und 4 aufgeteilt. Der Teilstrom 4 wird über einen Wärmetauscher 5 angewärmt und mit einer Temperatur von 80 bis 120 °C einer Hydrierstufe 6 mit drei Katalysatorbetten, die einen Nickel-Katalysator enthalten, aufgegeben. Der andere Teilstrom 3 wird auf die Hydrierstufe 6 verteilt. In der Hydrierstufe 6 werden die Aromaten zu Napthenen hydriert. Das erhaltene Produkt, das bis zu 40 Vol.% Aromaten enthalten kann, im vorliegenden Beispiel aber kleiner 0,5 Vol.% Aromaten aufweist, wird bei einer Temperatur von 120 bis 160 °C mittels Leitung 7 abgezogen, in den Wärmetauschern 5 und 8 abgekühlt, wobei der Wärmetauscher 8 mit Kühlwasser betrieben wird, und schließlich einer Gasflüssigtrennung 9 zugeführt. Flüssiges Produkt wird teilweise über Leitung 10 zurückgeführt und dient zur Verdünnung des Einsatzstoffes für die Hydrierstufe 6. Anfallendes Wasserstoffgas wird dem in einer Druckwechseladsorptionsanlage (PSA) 11 produzierten Wasserstoff zugemischt. Der die Naphthene enthaltende Produktstrom in Leitung 12 wird der in Figur 2 dargestellten isothermen Reaktionsstufe zugeleitet.The pretreatment stage shown in Figure 1 is used to hydrogenate the cyclic Feedstocks containing hydrocarbons. A stream of C5 + Hydrocarbons from an olefin plant undergo selective hydrogenation and Desulfurization and fractionation 1 fed. The pyrolysis heavy gasoline obtained with predominantly C7 + hydrocarbons has an aromatic content from typically 60 to 90% by volume, in the present example 87% by volume. through A pump 2 turns the pyrolysis heavy gasoline to a pressure of approx. 30 bar compressed and divided into two partial streams 3 and 4. The partial stream 4 is a Heat exchanger 5 heated and one with a temperature of 80 to 120 ° C. Hydrogenation stage 6 with three catalyst beds which contain a nickel catalyst, given up. The other partial stream 3 is distributed to the hydrogenation stage 6. In the Hydrogenation stage 6, the aromatics are hydrogenated to naphthenes. The product obtained, which can contain up to 40 vol.% aromatics, but smaller in the present example 0.5 vol.% Aromatics, is at a temperature of 120 to 160 ° C by means of Line 7 withdrawn, cooled in the heat exchangers 5 and 8, the Heat exchanger 8 is operated with cooling water, and finally one Gas-liquid separation 9 supplied. Liquid product is partly via line 10 recycled and serves to dilute the feedstock for hydrogenation stage 6. The resulting hydrogen gas is in a pressure swing adsorption system (PSA) 11 hydrogen produced were added. The product stream containing the naphthenes the isothermal reaction stage shown in FIG. 2 is fed in line 12.

Wie in Figur 2 gezeigt, wird der die Naphthene enthaltende Produktstrom mittels einer Pumpe 13 auf ca. 25 bis 70 bar, bevorzugt 50 bis 60 bar, im vorliegenden Beispiel auf ca. 60 bar verdichtet, mittels Wärmetauscher 14 und 15 vorgewärmt und einer Heizstufe 16 zugeführt. Die auf ca. 380 °C aufgeheizten Einsatzstoffe werden in den Isothermreaktor 17 eingeleitet. Im vorliegenden Ausführungsbeispiel ist der Isothermreaktor 17 als Geradrohr-Reaktor ausgeführt. Die im Reaktor 17 angeordneten Rohre werden mit einem Wärmeträgeröl von außen gekühlt, welches in der Leitung 18 zirkuliert. Die im Reaktor 17 anfallende Reaktionswärme wird mittels des Wärmeträgeröls an einen externen Dampferzeuger 19 abgeführt. Der Isothermreaktor 17 enthält einen Zeolith-Katalysator. In dem Reaktor werden die Naphthene unter isothermen Bedingungen bei einer gleichbleibend hohen Konversionsrate zu Paraffinen umgesetzt. Die Reaktionsprodukte werden über Leitung 20 abgeführt und mittels der Wärmetauscher 15 und 14 abgekühlt. Bei einer über dem Taupunkt liegenden Temperatur von 144 °C werden die Reaktionsprodukte an die in Figur 3 dargestellte Nachbearbeitungsstufe übergeben.As shown in Figure 2, the product stream containing the naphthenes is by means of a Pump 13 to about 25 to 70 bar, preferably 50 to 60 bar, in the present example compressed about 60 bar, preheated by means of heat exchangers 14 and 15 and one Heating level 16 supplied. The feed materials heated to approx. 380 ° C are used in the Isothermal reactor 17 initiated. In the present embodiment, the Isothermal reactor 17 designed as a straight tube reactor. The arranged in the reactor 17 Pipes are cooled from the outside with a heat transfer oil, which is in line 18 circulated. The heat of reaction occurring in the reactor 17 is by means of Heat transfer oil discharged to an external steam generator 19. The isothermal reactor 17 contains a zeolite catalyst. The naphthenes are placed in the reactor isothermal conditions with a constant high conversion rate to paraffins implemented. The reaction products are discharged via line 20 and by means of Heat exchangers 15 and 14 cooled. At one above the dew point Temperature of 144 ° C, the reaction products to that shown in Figure 3 Submit post processing level.

In der in Figur 3 dargestellten Nachbearbeitungsstufe werden die Reaktionsprodukte fraktioniert. Hierzu werden die Reaktionsprodukte über Leitung 21 einem Wäscher 22 zugeführt. Das gasförmige Produkt wird vom Kopf des Wäschers 22 mittels Leitung 23 abgeführt, in einem Wärmetauscher 24 gegen Kühlwasser gekühlt und einer Gas-Flüssigkeitstrennung 25 zugeführt. Das erhaltene gasförmige Produkt wird über Leitung 26 einer weiteren Gas-Flüssigkeitstrennstufe 27 zugeführt. Das in dieser Trennstufe anfallende gasförmige Produkt wird bei einer Temperatur von ca. 15 °C über einen Trockner 28 zu einem Plattenwärmetauscher 29 geleitet. In einer weiteren Gas-Flüssigkeitstrennstufe 30 wird gasförmiger Wasserstoff abgetrennt und mittels Leitung 31 in den Prozess zugeführt. Das in der Trennstufe 30 anfallende flüssige Produkt wird schließlich über Leitung 32 aus der Nachbehandlungsstufe abgeführt und steht als Einsatzstoff mit einem sehr hohen Paraffingehalt für den Steamcracker der Olefinanlage zur Verfügung. Das im Wäscher 22 anfallende Kondensat enthält teilweise Propan, und wird über Leitung 33 einer Propanausstrippung in einer Strippkolonne 34 zugeführt. Dabei anfallende Aromaten werden schließlich mittels einer Rückführleitung 35 zu der in Figur 1 dargestellten Vorbehandlungsstufe zurückgeführt.In the post-processing stage shown in Figure 3, the reaction products fractionated. For this purpose, the reaction products are passed to a scrubber 22 via line 21 fed. The gaseous product is discharged from the head of the scrubber 22 via line 23 dissipated, cooled in a heat exchanger 24 against cooling water and a gas-liquid separation 25 fed. The gaseous product obtained is about Line 26 fed to a further gas-liquid separation stage 27. That in this Separation stage resulting gaseous product is at a temperature of approx. 15 ° C passed through a dryer 28 to a plate heat exchanger 29. In another Gas-liquid separation stage 30, gaseous hydrogen is separated and by means of Line 31 fed into the process. The liquid obtained in the separation stage 30 The product is finally discharged from the aftertreatment stage via line 32 and stands as a feed with a very high paraffin content for the steam cracker Olefin plant available. The condensate obtained in the scrubber 22 contains partially propane, and is via line 33 of a propane stripping in a Stripping column 34 fed. Aromatics that are produced in the process are finally added a return line 35 to the pretreatment stage shown in FIG. 1 recycled.

In Figur 4 ist die Produktzusammensetzung des die Anlage verlassenden Produktstromes angegeben, der als Einsatz für den Steamcracker der Olefinanlage verwendet wird (SC-Feedstock).FIG. 4 shows the product composition of the product leaving the plant Product stream specified as the insert for the steam cracker of the olefin plant is used (SC feedstock).

Claims (6)

Verfahren zur Herstellung von Paraffinen aus zyklische Kohlenwasserstoffe enthaltenden Einsatzstoffen wie Mineralölfraktionen und/oder Fraktionen aus thermischen oder katalytischen Konversionsanlagen enthaltend Alkane, Alkene, zyklische Alkane und/oder Aromaten durch Umsetzen mit einem Zeolith-Katalysator, dadurch gekennzeichnet, dass die Umsetzung unter isothermen Bedingungen in einem gekühlten Reaktor durchgeführt wird.Process for the production of paraffins from feedstocks containing cyclic hydrocarbons such as mineral oil fractions and / or fractions from thermal or catalytic conversion plants containing alkanes, alkenes, cyclic alkanes and / or aromatics by reaction with a zeolite catalyst, characterized in that the reaction is carried out under isothermal conditions is carried out in a cooled reactor. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Umsetzung in von außen gekühlten Rohren des Reaktors durchgeführt wird.A method according to claim 1, characterized in that the reaction is carried out in externally cooled tubes of the reactor. Verfahren nach Anspruch 1, dadurch gekennzeichnet, dass die Umsetzung in einem Reaktor mit gewickelten Rohren durchgeführt wird.A method according to claim 1, characterized in that the reaction is carried out in a reactor with wound tubes. Verfahren nach einem der Ansprüche 1 bis 3, dadurch gekennzeichnet, dass die die zyklischen Kohlenwasserstoffe enthaltenden Einsatzstoffe in einer Vorbehandlungsstufe zu einem Einsatzstrom hydriert werden, der überwiegend Naphthene und bis zu 40 Vol.% Aromaten enthält.Method according to one of claims 1 to 3, characterized in that the feedstocks containing the cyclic hydrocarbons are hydrogenated in a pretreatment stage to a feed stream which predominantly contains naphthenes and up to 40% by volume of aromatics. Verfahren nach Anspruch 4, dadurch gekennzeichnet, dass der Einsatzstrom weniger als 5 % Aromaten enthält.A method according to claim 4, characterized in that the feed stream contains less than 5% aromatics. Verfahren nach einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, dass dem gekühlten Reaktor ein adiabates Katalysatorbett mit einem Hydrierkatalysator unmittelbar vorgeschaltet ist, wobei durch Hydrierung von Kohlenwasserstoffen anfallende Reaktionswärme zur Vorheizung der Einsatzstoffe für die anschließende Isothermreaktion eingesetzt wird.Process according to one of claims 1 to 5, characterized in that an adiabatic catalyst bed with a hydrogenation catalyst is connected directly upstream of the cooled reactor, heat of reaction generated by hydrogenation of hydrocarbons being used to preheat the starting materials for the subsequent isothermal reaction.
EP02018081A 2001-08-13 2002-08-13 Process for the preparation of paraffines from educts containing cyclic hydrocarbons Expired - Lifetime EP1285903B1 (en)

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EP02018081A Expired - Lifetime EP1285903B1 (en) 2001-08-13 2002-08-13 Process for the preparation of paraffines from educts containing cyclic hydrocarbons

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AT (1) ATE321014T1 (en)
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Cited By (1)

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Publication number Priority date Publication date Assignee Title
US10563130B2 (en) 2014-07-17 2020-02-18 Sabic Global Technologies B.V. Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process

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Publication number Priority date Publication date Assignee Title
WO1993008145A1 (en) * 1991-10-25 1993-04-29 Mobil Oil Corporation Combined paraffin isomerization/ring opening process
WO2001027223A1 (en) * 1999-10-13 2001-04-19 Veba Oil Refining & Petrochemicals Gmbh Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1993008145A1 (en) * 1991-10-25 1993-04-29 Mobil Oil Corporation Combined paraffin isomerization/ring opening process
WO2001027223A1 (en) * 1999-10-13 2001-04-19 Veba Oil Refining & Petrochemicals Gmbh Method for production of n-alkanes from mineral oil fractions and catalyst for carrying out said method

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10563130B2 (en) 2014-07-17 2020-02-18 Sabic Global Technologies B.V. Upgrading hydrogen deficient streams using hydrogen donor streams in a hydropyrolysis process

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DE50206118D1 (en) 2006-05-11
ATE321014T1 (en) 2006-04-15
DE10139726A1 (en) 2003-02-27
EP1285903B1 (en) 2006-03-22

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