EP3137577B1 - Method for obtaining crude oil products - Google Patents

Description

The invention relates to a process for the production of crude oil products.

State of the art

Crude oil is first desalinated in known refinery processes and, after heating, subjected to fractional distillation at atmospheric pressure (hereinafter referred to as atmospheric distillation). The remaining so-called atmospheric residue is fed to a vacuum distillation.

However, not all of the fractions obtained in atmospheric distillation and vacuum distillation are profitable. A part of the compounds contained therein can therefore be catalytically converted, for example, and upgraded in this way. However, this does not always succeed completely. A thermal conversion of crude oil components by steam cracking (engl. Steam Cracking) is also known.

The object of the invention is to improve corresponding methods and devices and in particular to increase the yield of high-grade crude oil products.

Disclosure of the invention

This object is achieved by a method having the features of patent claim 1. Embodiments are the subject of the respective subclaims and the following description.

Reference should be made to the relevant technical literature for the terms used below and technical details of the methods used (see, for example, US Pat Zimmermann, H. and Walzl, R .: Ethylene, In: Ullmann's Encyclopedia of Industrial Chemistry, Weinheim: Wiley-VCH, Online Publication 2007, DOI: 10.1002 / 14356007.a10_045.pub2 , such as Irion, WW and Neuwirth, OS: Oil Refining, In: Ullmann's Encyclopedia of Industrial Chemistry, Weinheim: Wiley-VCH, Online Publication 2000, DOI: 10.1002 / 14356007.a18_051 ).

Steam cracking processes are generally carried out by means of tube reactors whose reaction tubes, the so-called coils, can be operated individually or in groups under the same or different conditions. Reaction tubes operated under identical or comparable conditions or groups of reaction tubes, but also tube reactors operated under uniform conditions, are referred to below as "cracking furnaces". In the language used here, a cracking furnace is therefore a structural unit used for steam cracking in which identical or comparable reaction conditions are present. A steam cracking plant may comprise one or more cracking furnaces.

A fission gas stream is understood here to mean a gaseous stream which is formed from the effluent of one or more cracking furnaces. The cracked gas stream (also referred to as cracker effluent) in a first cooling step is typically quenched in a quench cooler, such as a transfer line exchanger (TLE) with cooling water and then in a second quenching step, i. Mix with a liquid hydrocarbon stream, cooled.

In the literature sometimes the first cooling step, ie the cooling of the quenching gas with cooling water, for example in the quench cooler, is referred to as quenching. However, in this first cooling step, the cracked gas is only indirectly cooled and not mixed, as in the second cooling step, with a liquid hydrocarbon stream. The second cooling step may therefore also be referred to as oil quench for better distinctness. The stream formed by combining the cracked gas stream with the liquid stream used for quenching is referred to herein as quench effluent. The "quench effluent" comprises all of the liquid stream used for quenching and compounds derived from the cracked gas stream which are reduced at most by corresponding reaction products due to the quench. In particular, the mass flow of the quench effluent corresponds to the sum of the mass flow of the liquid stream used for quenching and the mass flow of the cracked gas stream, It is therefore explicitly not the product of a separation or deposition process. The quench effluent is present immediately after the union of the quench liquid stream and the split gas stream.

Advantages of the invention

The invention proposes a process for recovering crude oil products in which a gaseous stream is formed by evaporation from a stream of crude oil and the gaseous stream is subjected at least in part to a steam cracking process. In the steam cracking process, a split gas flow is generated. Corresponding methods are for example from US 2008/0221378 A1 and the WO 2010/117401 A1 known.

In the context of the present invention, at least part of the gaseous stream formed during the evaporation of the crude oil may be supplied to one or more cracking furnaces alone or after being combined with one or more further streams, for example one or more recycle streams. If several cracking furnaces are present, they can also be charged with different currents. As is generally known, the charging of the cracking furnaces takes place in each case after the addition of water vapor.

The resulting cracked gas stream is at least partially quenched to give a quench effluent stream with a liquid hydrocarbon stream. The present invention proposes to use a fraction of the crude oil stream which remains liquid during the evaporation of the crude oil stream, at least in part to form the liquid hydrocarbon stream used for quenching, wherein the liquid hydrocarbon stream used for quenching is poor or free of components which originate from the Quenchabstrom or a stream formed from the Quenchabstrom were separated. Further, the quench effluent is obtained by quenching with the liquid hydrocarbon stream at a temperature ranging from 0 to 250 ° C.

In other words, in the present invention, the liquid hydrocarbon stream used for quenching is not formed using a recycle stream and no quenching cycle is used as it is conventional method is known. In a quenching cycle of a conventional method, for example, a so-called oil column with two sections arranged one above the other is used. The quench oil is given up at the top of the lower section. In a lower portion of the lower portion of the cracked gas stream is fed and sent towards the Quenchöl. In the gap gas stream contained heavy compounds are dissolved or suspended in the quench oil and the gap gas stream is cooled simultaneously. The quench oil with the optionally dissolved or suspended therein compounds is withdrawn from the bottom of the oil column, optionally treated, and returned to the head of the lower portion of the oil column again. In an upper region of the oil column pyrolysis gasoline is abandoned, which is separated in a downstream water quench and also partially circulated.

However, the disadvantage of conventional quench circuits is the aging of the quench oil. Due to the frequent contacts with the hot cleavage gas stream, the initially low-viscosity compounds are polymerized and the formation of soot and tar or other tough, high-boiling compounds occurs. The quench oil must therefore be replaced regularly and replaced by fresh quench oil conventionally. The aged quench oil is practically worthless. In contrast, the liquid hydrocarbon stream used for quenching is poor in or free of components separated from the quench effluent or stream formed from the quench effluent, undergoing little or no aging because the products contained therein are not recycled Connections come into contact with the gap gas flow just once. This one-time contact does not lead to aging reactions and the corresponding compounds can be converted into product fractions which can still be used profitably.

The split gas stream exits the radiation zone of the cracking furnace (s) at a temperature of typically 750 to 875 ° C. The collapsed gas stream should be cooled as quickly as possible to avoid further reaction of the compounds formed, for example polymer formation. If the above-mentioned linear coolers are used, they perform a considerable part of the cooling of the cracked gas stream. As in the article cited above " Ethylene "in Ullmann's Encyclopedia of Industrial Chemistry , the split gas flow occurs conventionally still with a temperature of about 230 ° C in the oil column and leaves it at a temperature of about 100 ° C. The majority of the heat is dissipated by the quench oil. When using a corresponding conventional oil quench so the temperature of the quenching gas is reduced from a temperature value in a first temperature range to a temperature value in a second temperature range, wherein the temperature value in the second temperature range is about 130 ° C lower than the temperature value in the first temperature range , In processes without the use of a linear cooler, the temperature difference between the temperature values is significantly higher.

From the US 2008/0221378 A1 For example, a method is known in which an unvaporized portion of a crude oil stream is used for a pre-quench of a cracked gas stream obtained by steam cracking a vaporized portion of the crude oil stream. The pre-quench is made to cleave, but still cleavable components contained in the non-evaporated portion by the heat of the cracked gas stream. The addition of the unevaporated fraction to the cracked gas stream in the course of the pre-quenching therefore takes place at a still high temperature of the cracked gas stream, typically at 760 to 929 ° C. At the same time, the pre-quench reduces the temperature of the cracked gas stream only slightly, namely by typically not more than 111 ° C. Downstream of the pre-quenching, the current obtained is therefore still at a very high temperature, which requires a further quench before further processing. In other words, in the method according to the US 2008/0221378 A1 the temperature of the quench gas in the prequench decreases from a temperature value in a first temperature range to a temperature value in a second temperature range, wherein the temperature value in the second temperature range is at most 111 ° C lower than the temperature value in the first temperature range. The temperature value in the second temperature range is at least 649 ° C.

In contrast, by quenching with the liquid hydrocarbon stream according to the invention, the quench effluent, as mentioned, is obtained at a temperature which is in a temperature range of 0 to 250 ° C. The temperature can be in particular in a temperature range of 50 to 200 ° C or from 50 to 150 ° C, ie at a temperature which is also achieved in a conventional oil column, and allows direct processing of Quenchabstroms.

Advantageously, in this case, the cracked gas stream, before it is quenched with the liquid hydrocarbon stream, for example by means of a linear cooler, has already been cooled to a temperature which is 50 to 200 ° C, for example 100 to 150 ° C, above the temperature of Quenchabstr oms and, for example, corresponds to the typical inlet temperatures into an oil column in a conventional process. The invention makes it possible in this particularly preferred embodiment to dispense with the use of further quench oil, in particular an oil circuit. For this purpose, starting from the US 2008/0221378 A1 no reason, because it teaches that a high temperature of the cracked gas stream is required to crack compounds contained in the unevaporated portion of the crude oil stream. However, by a simple quench to low temperatures by means of this non-vaporized portion, corresponding cleavage reactions would be halted and a significant gap yield would not be achievable. Therefore, a high temperature of the effluent of the pre-quenching, and thus another quench in the form of an oil circuit, is mandatory here.

Since the Quenchabstrom contains a considerable proportion of finely divided oil droplets from the quenching liquid stream and heavy components (oils, tars and the like), it is first freed in conventional steam cracking process in a so-called oil column of corresponding components. Only downstream of the oil column, a corresponding stream of the known separation stages for recovering the hydrocarbon products from the cracking gas can be supplied.

The present invention is based on the idea of dispensing with a corresponding oil column and of further processing the quench effluent, for example as in conventional crude oil processing. This is possible because, by quenching with the remaining liquid in the evaporation of the crude oil stream, or a corresponding part thereof, in the Quenchabstrom only those (heavier) components are included, as they are found in conventional crude oil streams, the atmospheric distillation be subjected.

In contrast to conventional methods in which a Quenchölkreislauf is provided, so used in the present invention, the liquid hydrocarbon stream used for quenching only once for quenching.

A great advantage of the proposed method is therefore that no oil circuit is required for the quench, in which the oil (ie, the liquid hydrocarbon stream conventionally used for quenching) usually ages very much by chemical reactions, in particular significantly increases in viscosity, and thereby loses value. In the context of the present invention, such aging reactions do not play a role for the reasons explained. Another advantage that results from not using an oil circuit, is that, for example, the conventionally provided heat recovery from the cracking gas eliminated by consuming heat ashtray in the oil circuit and the heat can be fed via the Quenchabstrom directly another consumer. The heat can be used, for example, for (pre) heating the streams used in the atmospheric distillation. Also, the remaining in the evaporation of the crude oil stream liquid fraction can be cooled before use, with its heat can be transferred to other streams.

With particular advantage, therefore, in the context of the present invention, at least part of the quench effluent is used to form a separation insert, which is separated by distillation together with another stream of crude oil to obtain distillation effluents. This distillative separation is advantageously carried out initially in a distillation column for fractional distillation at atmospheric distillation, as it is also used in a conventional refinery. The atmospheric distillation may be followed by a vacuum distillation in a distillation column equipped therefor. All streams (cuts, fractions) formed in the distillation (for example, atmospheric distillation and / or vacuum distillation) are referred to herein as distillation effluents.

The separation insert may be formed from the quench effluent in any manner, but always contains hydrocarbons having one, two, three, four and more carbon atoms and / or hydrocarbons contained in the quench effluent, for example hydrocarbons formed by hydrogenation or further reactions after quenching. These are, for example, methane, ethane, ethylene, acetylene, propane, propylene and methylacetylene and saturated and unsaturated hydrocarbons having four carbon atoms. The mentioned "education" of the separation insert, for example, by separating a partial flow, combining with another stream or chemical and / or physical reacting done.

Further, the separation insert advantageously contains hydrocarbons previously contained in the quench liquid hydrocarbon stream or compounds formed from such hydrocarbons. These are typically hydrocarbons with more than ten or 20 and for example up to 30 or more carbon atoms. Such hydrocarbons thus need not advantageously be separated from the Quenchabstrom but are supplied in accordance with an advantageous embodiment of the method, in particular unchanged a common distillative separation together with the second crude oil stream.

In other words, an embodiment is proposed in which a common distillative separation of the Quenchabstroms is made together with the second crude oil stream. As a result, as explained below, a full integration into a refinery is achieved, for example, by the Quenchabstrom is completely supplied to an atmospheric distillation in a correspondingly equipped distillation column together with the second crude oil stream. This makes it possible to dispense with separate separation means for hydrocarbons in the steam gap stream or the Quenchabstrom. For example, the quench effluent together with the liquid hydrocarbon stream used for quenching can be transferred to a corresponding distillation column in which the usual crude oil fractions are recovered. The compounds contained in the liquid hydrocarbon stream used for quenching pass into the respective fractions, for example the vacuum gas oil or the atmospheric gas oil, according to their boiling point. Separate separation of the compounds contained in the liquid hydrocarbon stream used for quenching in the manner of a conventional oil column is therefore not required. A water quench is also eliminated since pyrolysis gasoline also passes into the corresponding fractions of the crude oil distillation, namely the gasoline fractions. A separate compression of Quenchabstroms is also not required.

The method can therefore be realized with significantly lower expenditure on equipment than a method of the prior art, as for example in the US 2009/0050523 A1 and in which only heavy fractions separated from a cracked gas in a conventional manner are fed to a refinery process. Starting from the US 2009/0050523 A1 is the method of the invention not obvious, because in the US 2009/0050523 A1 used Quenchöl- and pyrolysis gasoline cycle requires a separation of quench oil and pyrolysis gasoline. It is therefore not possible to transfer corresponding compounds in a quench effluent to a common separation with a second crude oil stream. The same applies with respect to a method, as for example in the US 2007/0055087 A1 is shown. The US 2010/0320119 A1 discloses a process in which a quench effluent is fed to a primary fraction to give different streams. Because the US 2010/0320119 A1 However, explicitly teaches to prepare a tar stream from the primary fractionation and use in a Quenchölkreislauf, here prohibits the feed of a second crude oil stream in the primary fractionation, because this would make it impossible to obtain the tar stream through the additionally fed crude oil components.

In other words, the present invention proposes, in an advantageous embodiment, to process the separation insert formed using the Quenchabstroms, like conventional crude oil streams, first in an atmospheric distillation. In atmospheric distillation, the products of the steam cracking process, such as ethylene and other light hydrocarbons, pass into the top stream of the distillation column. At the same time, the classical sections of the crude oil stream (and the liquid stream used for quenching) can be produced in this distillation column.

In the context of this preferred embodiment of the present invention, therefore, the oil column conventionally used in a steam cracking process and the distillation column used for atmospheric distillation in a conventional refinery process are functionally combined. The products of the steam cracking process withdrawn from the top or from the top of the atmospheric distillation column may be subjected, together with corresponding light products from the crude oil stream, if present, to the post-cracking gas separation steps usually following the oil column of a steam cracking process.

For example, in this case, first of all a water wash can be used, in which the naphtha which may possibly still be contained in a corresponding stream is deposited in liquid form. After washing with water, hydrocarbons having one to four carbon atoms typically remain in the gas phase. These can then be subjected to known separation sequences (Demethanizer First, Deethanizer First, etc., for details, see the cited technical literature).

The resulting in the column for atmospheric distillation further distillation effluents are composed of heavier hydrocarbons, which originate mainly from the uncleaved crude oil or the liquid used for quenching. These are, for example, so-called atmospheric gas oil (English: Atmospheric Gas Oil, AGO) and the mentioned atmospheric residues.

Further advantages can be achieved if certain hydrocarbons, for example contained in the cracked gas or in the further crude oil stream, are again subjected to the steam cracking process. Such streams subjected to the steam cracking process are referred to as recycle streams. Recycled streams can be combined and fed together or separately, possibly together with fresh inserts, identical or different cracking furnaces. As a fresh use of the present invention, the already explained, formed in the evaporation of the crude oil stream gaseous stream is used, but it can also be used other, supplied from the plant boundary streams.

The separation of the fractions provided as recycle streams can be carried out, for example, in the customary separation devices which are provided in the context of the present invention, similar to conventional steam-splitting processes. Separate separation of corresponding light fractions, as conventionally carried out in a refinery, can therefore be dispensed with. Such light fractions, because they can be fed to the steam cracking process as recycle streams, need not be stored in tanks as in conventional refinery plants. As also explained below, the compounds contained in corresponding streams can also be at least partially further implemented.

Overall, the measures according to the invention provide the advantage that it is possible to dispense with an oil column, and that no pyrolysis oil and no pyrolysis gasoline are produced as separate products. The compounds which conventionally pass into the pyrolysis oil and the pyrolysis gasoline are found again in the use of the process according to the invention in the corresponding distillation effluents (for example from the atmospheric distillation and the vacuum distillation).

The process according to the invention can also be configured by recycling all distillation effluents which are not desired as products, such that production of typical refinery products such as gasoline, diesel, heating oil etc. no longer occurs. The said components may be used, for example after appropriate treatment such as hydrotreats or (mild) hydrocracking, together or separately, as an insert for the steam cracking process. In such a case, for example, exclusively ethylene, propylene, butadiene, aromatics and high-pressure steam or electricity can be obtained from the crude oil used. This variant proves to be extremely economical. The method according to the invention can be flexibly adapted to the respective requirements of corresponding compounds.

The present invention further enables a particularly effective utilization of the waste heat generated in a steam cracking process. This can first be used to preheat the crude oil stream, the vaporized portion of which is then subjected to the steam cracking process. Further waste heat may, for example, also be used to heat the further stream of crude oil, which is then fed to the distillation column for atmospheric distillation. Overall, this results in an advantageous energy integration and a reduction in the dissipated waste heat. Also, the quench cooler can be integrated into a corresponding heat recovery circuit, for example, by steam generated there is used to heat the crude oil stream.

The separation by distillation of the separating insert formed using the Quenchabstroms together with the other crude oil is carried out, as explained, advantageously initially at atmospheric pressure and then in vacuo, so that recourse to known methods of refinery technology for distillation can be used and appropriate processes for the treatment of the distillation effluents can be used.

As already mentioned, the distillation effluents or streams derived therefrom may also be at least partially subjected to the steam cracking process. In each case, diverted streams can be formed in each case by branching off a partial stream, combining with other streams, chemically or physically reacting at least some components in appropriate streams, heating, cooling, evaporating, condensing, etc.

With particular advantage corresponding derived streams can be formed by hydrocracking. In such processes, the distillation effluents, if appropriate after prior further separation and / or treatment, are partially or fully catalytically hydrogenated and at least partially cracked. In this way, as furnace inserts, undesired unsaturated hydrocarbons can be converted to saturated hydrocarbons and reacted again to form value products in the steam cracking process.

The recycled streams may in particular be hydrotreated and / or hydrocracked atmospheric gas oil (English: Atmospheric Gasoil, AGO) and treated by hydrotreatment and / or hydrocracked vacuum gas oil (Vacuum Gasoil, VGO), ie distillation residues from atmospheric distillation or Act vacuum distillation. Suitable recycling streams are also unsaturated hydrocarbons having two to four carbon atoms and / or hydrocarbons having five to eight carbon atoms in question. Naphtha can also be used again in corresponding steam cracking processes.

In the distillation separation downstream separation stages, which are subjected to hydrocarbons having two to four carbon atoms, for example, compounds such as methane, ethylene, propylene, butadiene and / or aromatics (benzene, toluene and / or xylenes, collectively referred to as BTX) recovered and from the system are running. The vacuum residue obtained in the vacuum distillation and which can no longer be used and / or the methane formed can be burned to produce energy.

A plant for recovering crude oil products, which is adapted to form a gaseous stream from a crude oil stream by evaporation and to subject the gaseous stream at least in part to a steam cracking process, may be arranged such that in the steam cracking process, a cracked gas stream is generated at least in part to quench a Quenchabstroms with a liquid hydrocarbon stream can be quenched. Means may be provided which are adapted to use, at least in part, a portion of the crude oil stream remaining on evaporation of the crude oil stream to form the liquid hydrocarbon stream used for quenching. The quench liquid hydrocarbon stream is lean or free of components separated from the quench effluent or stream formed from the quench effluent stream. Further, the quench effluent is obtained by quenching with the liquid hydrocarbon stream at a temperature ranging from 0 to 250 ° C.

Such a system has all the means that enable it to carry out a method according to the invention. Advantageously, the plant comprises at least one distillation column adapted for fractional distillation at atmospheric pressure and means adapted to supply to said distillation column a separation insert formed using at least a portion of the quench effluent and another crude stream.

Advantageously, means are furthermore provided which are set up to at least partially subject the distillation effluents or streams derived therefrom formed in this distillation column to the steam cracking process.

The invention will be explained in more detail with reference to the accompanying drawings, which show preferred embodiments of the invention.

Figur 1

zeigt eine Anlage zur Gewinnung von Rohölprodukten in Teilansicht.

Figur 2

zeigt eine Anlage zur Gewinnung von Rohölprodukten in erweiterter Ansicht.

Brief description of the drawings

FIG. 1

shows a plant for the production of crude oil products in partial view.

FIG. 2

shows a plant for the extraction of crude oil products in an expanded view.

In the figures, corresponding elements are given identical reference numerals and will not be explained repeatedly. The plant components shown correspond to the same steps of a process.

Embodiments of the invention

In FIG. 1 is a plant for the production of crude oil products shown schematically in a partial view and designated 100 in total.

The plant 100 supplied crude oil a is divided into two crude oil streams b and c. The crude oil stream b is preheated in a convection zone of one or more cracking furnaces 1 and transferred to an evaporation tank 2. A proportion of the crude oil stream b evaporating in the evaporation vessel 2 is conducted as stream d after mixing with steam through the radiation zone of the cracking furnace 1 or furnaces, a gap gas e being obtained.

The cracked gas e is cooled in a quench cooler 3 and then quenched in a quench device 4 with a portion of the crude oil stream b remaining liquid in the evaporation tank 2, here illustrated with stream f. A separating insert formed from the quenching stream g (without a separate name) is transferred to a distillation column 5 for fractional atmospheric distillation, into which the crude oil stream c is also fed.

The distillation column 5 is operated in a conventional manner, so that in this example, an atmospheric residue h and an atmospheric gas oil i are obtained. From the top of or from an upper portion of the distillation column 5, a stream k is withdrawn containing light products from the cracking furnace (s) 1 and the crude oil stream c. By mixing water (not shown) in a water scrubber 6, a water-naphtha mixture is separated from the stream k and transferred as stream I into a decanter 7. In this a water flow m and a naphtha flow n is obtained.

In the water scrubber 6 gaseous remaining fractions, which are essentially hydrocarbons having one to four carbon atoms, are withdrawn as stream o and fed to a decomposition part, which may be formed in a known manner. In a corresponding decomposition part, for example, first a separation of methane and / or methane and ethane can be carried out (so-called Demethanizer First or Deethanizer First method).

In FIG. 2 is the plant 100 in an expanded view, ie as an enlarged section of an entire plant 100, illustrated and designated 200 in total. The Indian FIG. 1 Plant part shown, so at least one cracking furnace 1 with the associated facilities 2 to 4 and furnished for fractional atmospheric distillation distillation column 5 with a water scrubber 6 and an associated decanter 7, designated 100.

As in FIG. 2 1, a vacuum residue p is obtained from an atmospheric residue withdrawn as stream h from the distillation column 5 in a distillation column 8 equipped for vacuum distillation, which is fired in a device 9 and used to obtain energy, here indicated by arrow q can be.

A top stream r from the distillation column 8, so-called vacuum gas oil, is transferred to a hydrogenation unit 10, where the stream r can be processed by hydrocracking, for example. A correspondingly processed stream s can be returned to the steam cracking process or into one or more cracking furnaces 1. The same applies to the above-explained stream i, the atmospheric gas oil, which can be treated in a hydrogenation unit 11 and subsequently recycled as stream t into the steam cracking process. From a stream u, which contains substantially hydrocarbons having five to eight carbon atoms, aromatics can be separated in an aromatic extraction unit 12 and carried out as stream v from the plant. A remaining portion may be re-subjected as stream w to the steam cracking process. The already explained stream o, which predominantly has hydrocarbons having one to four carbon atoms, can be converted into a C4 decomposition part 13, in which the product streams indicated here overall with x, for example ethylene, propylene and butadiene, can be separated off. A methane stream y can be carried out from the plant and / or used for heating. Not obtained as product streams x Hydrocarbons can be recycled as stream z in the steam cracking process.

Claims (8)

1. Process for obtaining crude oil products, in which a gaseous stream (d) is formed by evaporation (2) from a crude oil stream (b) and the gaseous stream (d) is at least partly subjected to a steamcracking process (1), wherein the steamcracking process (1) produces a cracking gas stream (e) which is at least partly quenched with a liquid hydrocarbon stream (f) to obtain a quench output stream (g), characterized in that a proportion (f) that remains in liquid form in the evaporation (2) of the crude oil stream (b) is at least partly used to form the liquid hydrocarbon stream (f) used for quenching, wherein the liquid hydrocarbon stream used for quenching has a low level of or is free of components that have been separated from the quench output stream (g) or a stream formed from the quench output stream (g) and the quench output stream (g) is obtained by quenching with the liquid hydrocarbon stream (f) at a temperature lying in a temperature range of from 0 to 250°C.
2. Process according to Claim 1, in which a separation feed is formed from at least a portion of the quench output stream (g) and is distillatively separated (5, 8) together with a further crude oil stream (c) to obtain distillation output streams (h, i, k, p, r).
3. Process according to Claim 2, in which the distillation output streams (h, i, k, p, r) or streams derived therefrom (s, t, w, z) are subjected to the steamcracking process (1) at least partly as recycle streams.
4. Process according to either of Claims 2 and 3, in which the distillative separation (5, 8) of the separation feed together with the further crude oil stream (c) is effected first at atmospheric pressure (5) and then under reduced pressure (8).
5. Process according to Claim 3 or 4, in which streams (s, t) derived from at least a portion of the distillation output streams (i, r) at least by catalytic hydrogenation (10, 11) are formed.
6. Process according to any of Claims 3 to 5, in which atmospheric gas oil (i) treated by catalytic hydrogenation (11), catalytic hydrogenation-treated vacuum gas oil (r), saturated hydrocarbons having two to four carbon atoms (z) and/or hydrocarbons having five to eight carbon atoms (w) are used as recycle streams.
7. Process according to any of Claims 2 to 6, in which methane, ethylene, propylene and/or butadiene (x) and/or aromatic compounds (v) are obtained.
8. Process according to any of Claims 2 to 7, in which at least a portion of the distillation output streams (p, y) is burned for energy generation.

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