EP3137578A1

EP3137578A1 - Method and plant for obtaining crude oil products

Info

Publication number: EP3137578A1
Application number: EP15721173.1A
Authority: EP
Inventors: Heinz Zimmermann
Original assignee: Linde GmbH
Current assignee: Linde GmbH
Priority date: 2014-04-30
Filing date: 2015-04-28
Publication date: 2017-03-08
Anticipated expiration: 2035-04-28
Also published as: KR20160146766A; AU2015254695A1; WO2015165921A1; BR112016025290A2; CN106232779A; JP2017516893A; US20170058215A1; RU2016142702A; EP3137578B1; RU2016142702A3; PH12016501940A1; CN106232779B; HUE039134T2; US10000711B2

Abstract

A method is disclosed for obtaining crude oil products, wherein a gaseous stream (d) is formed from a first crude oil stream (b) and the gaseous stream (d) undergoes, at least partially, a steam cracking process (1), wherein in the steam cracking process (1) a cracking gas stream (e) is produced, which is quenched at least partially with a fluid hydrocarbon stream (f) while maintaining a quench outflow (g). This involves using at least a part of the quench outflow (g) to form a separation feed and the separation feed is separated out by distillation (5, 8) together with a second crude oil stream (c) while maintaining distillation outflows (h, i, k, p, r). The separation feed is formed in such a way that it contains hydrocarbons contained in the quench outflow (g) with one, two, three, four and more carbon atoms and/or hydrocarbons formed from such hydrocarbons. The invention likewise relates to a plant (100) configured for carrying out the method.

Description

description

Process and plant for the extraction of crude oil products

The invention relates to a method and a plant for the production of

Crude oil products according to the preambles of the independent claims.

State of the art

Crude oil is first desalinated in known refinery processes and after heating a 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 and a system according to the features of the independent claims. Embodiments are the subject of the respective subclaims and the following description. For the terms used below and technical details of the

refer to relevant literature (see

For example, 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, and 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. Operated under the same or similar conditions

Reaction tubes or groups of reaction tubes, but also operated under uniform conditions tubular reactors in total, are referred to below as each 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) is typically used in a quench gas cooler, for example a linear cooler (transfer line

Exchanger, TLE) with cooling water and then in a second cooling step by quenching, i. Mix with a liquid hydrocarbon stream, cooled.

In the literature, sometimes the first cooling step, i. the cooling of the quenching gas with cooling water, for example in the quench cooler, referred to as quenching. In this first cooling step, however, the cracked gas is cooled only indirectly and not, as in the second cooling step, with a liquid

Hydrocarbon Ström mixed. 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 stream" comprises all of the liquid stream used for quenching and compounds derived from the cracked gas stream which may at most be equivalent

Reaction products are reduced 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 Quenchabstrom is immediately after the union of the quenching

used liquid stream and the split gas stream before. Advantages of the invention

The invention proposes a method for recovering crude oil products in which a gaseous stream is formed from a first crude oil stream and the gaseous stream is at least partially subjected to a steam cracking process. In the steam cracking process, a split gas flow is generated.

In the context of the present invention, at least a part of the at

Evaporation of the crude formed gaseous stream alone or after

Association with one or more further streams, for example, one or more recycle streams, one or more cracking furnaces are supplied. 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 cleavage gas stream is at least partially to obtain a

Quenchabstroms quenched with a liquid hydrocarbon stream. The present invention proposes to use at least part of the quench effluent to form a separation insert and to separate the separation insert together with a second crude oil stream to obtain distillate effluents by distillation. The separation insert may be formed from the quench effluent in any manner, but always contains within the quench effluent

Hydrocarbons having one, two, three, four or more carbon atoms and / or from such hydrocarbons, for example by hydrogenating or

Further reactions after quenching formed hydrocarbons. 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 can

for example, by separating a partial flow, merging 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 and / or compounds formed from such hydrocarbons. These are typically hydrocarbons with more than ten or twenty and more

for example, up to 30 or more carbon atoms. Thus, such hydrocarbons advantageously do not need to be separated from the quench effluent, but according to an advantageous embodiment of the method

in particular, unchanged supplied to a common distillative separation together with the second crude oil stream.

In other words, it is proposed in the context of the present invention, a common distillative separation of Quenchabstroms or the separation insert formed using the Quenchabstroms and thus also lighter

Make hydrocarbons together with the second crude oil stream. As explained below, the present invention achieves full integration into a refinery by, for example, feeding the quench effluent or separation feedstock entirely to atmospheric distillation in a correspondingly configured distillation column along with the second crude stream. This makes it possible to dispense with separate separation means for hydrocarbons in the steam gap stream or the Quenchabstrom. For example, the Quenchabstrom or the separation insert together with the quenching

used liquid hydrocarbon Ström in a corresponding

Are transferred to the 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. A separate separation of the liquid used in the quenching

Hydrocarbon Ström compounds contained in the manner of a conventional oil column is 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 in the invention.

The inventive method can therefore be with significantly less

implement equipment effort as a method of the prior art, as it For example, in US 2009/0050523 A1, and in which only in a conventional manner separated from a cracked gas heavy fractions are fed to a refinery process. Starting from US 2009/0050523 A1, the process according to the invention is not obvious since the quench oil and pyrolysis benzene circulation used in US 2009/0050523 A1 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 regard to a method, as shown for example in US 2007/0055087 A1. US 2010/03201 19 A1 discloses a method in which a quench effluent is fed to a primary fractionation to obtain different streams. However, since US 2010/03201 19 A1 explicitly teaches to prepare a tar stream from the primary fractionation and to use it in a quench oil cycle, the introduction of a second crude oil stream into the primary fractionation is prohibited since this would make it impossible to obtain the tar stream by the additionally fed crude oil components , 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 vapor 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.

According to the invention, however, the said components from the

Quenchabstrom in the subsequent distillation separation, the

Quenchabstrom is subjected together with the second crude oil stream, removed and go into the appropriate (s) fraction (s).

A particularly advantageous embodiment of the invention provides to form said gaseous stream by evaporation from the first crude oil stream, wherein a portion of the crude oil stream remaining liquid during the evaporation is used at least in part to form the liquid hydrocarbon stream used for quenching. It is particularly advantageous if the liquid hydrocarbon stream used for quenching is poor or free of components which have been separated off from the quench waste stream or a stream formed from the quench waste stream. In other words, in the context of the present invention, the liquid hydrocarbon stream used for quenching is advantageously not submerged Use of a recycle stream formed and there is no Quenchkreislauf used, as it is known from conventional methods. 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 be replaced. The aged quench oil is practically worthless. In contrast, the liquid hydrocarbon stream used according to the preferred embodiment for quenching is poor in or free of components separated from the quench effluent stream or a stream formed from the quench effluent, with little or no aging process because it is lean or free from components contained, not recycled compounds only once with the

Spaltgasstrom come into contact. This one-time contact does not lead to aging reactions and the corresponding compounds can in

Product fractions are transferred, which can be used profitably. The split gas stream leaves the radiation zone of the cracking furnace (s) at a temperature of typically 750 to 875 Ό. The splashing gas flow should be for

Prevention of further reaction of the compounds formed, for example a polymer formation, are cooled as quickly as possible. If the above-mentioned linear coolers used, these lead a considerable part of

Cooling of the cracked gas flow through. As in the article cited above "Ethylene" In Ullmann's Encyclopaedia of Industrial Chemistry, the cracked gas stream conventionally enters the oil column at a temperature of about 230 ° C. 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 by about 130 Ό I¬ 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 US 2008/0221378 A1 a method is known in which a non-vaporized 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 we d through the prequench the

Temperature of the fission gas stream only slightly reduced, namely by typically not more than 1 1 1 Ό. 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 US 2008/0221378 A1, the temperature of the quenching gas in the preamble 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 at most 1 1 1 Ό 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 the advantageous quenching with the liquid

Hydrocarbon ström the Quenchabstrom obtained at a temperature which is in a temperature range of 0 to 250 Ό, in particular from 50 to 200 Ό or from 50 to 150 Ό, ie at a temperature which is also achieved in a conventional oil column, and the a direct further processing of Quenchabstroms allows. Advantageously, in this case, the cracked gas stream, before it is quenched with the liquid hydrocarbon Ström, has already been cooled to a temperature which is 50 to 200 Ό, for example 100 to 150 Ό, above the temperature of Quenchabstroms and for example the typical

Incoming temperatures corresponds to an oil column in a conventional method. 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 this teaches that a high temperature of the cracked gas stream is required to split in the unevaporated fraction of the crude oil stream contained compounds. 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.

By quenching with the liquid fraction remaining at the evaporation of the crude oil stream, or a corresponding part thereof, in the Quenchabstrom only those (heavier) components are contained, as they are also found in conventional crude oil streams, which are subjected to atmospheric distillation. The remaining in the evaporation of the crude oil stream liquid fraction can also be cooled before its use, with its heat can be transferred to other streams. In contrast to conventional methods in which a quench oil circuit is provided, in this embodiment of the invention, therefore, the liquid hydrocarbon stream used for quenching is used only once for quenching. A big advantage of this process variant is therefore that no oil circuit is needed for the quench, in which the oil by chemical reactions

usually ages very much, increases strongly in viscosity, and thus loses much of its value. In the said process variant, 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 by consuming

Heat exchanger in the oil circuit is eliminated and the heat through the Quenchabstrom directly can be supplied to another consumer. The heat can be used, for example, for (pre) heating the streams used in the atmospheric distillation. As mentioned, in the context of the present invention, the separating insert is formed from at least part of the quenching flow, which, together with the second

Crude oil is separated by distillation 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 a vacuum distillation set up in a dedicated

Connect the distillation column. All streams (cuts, fractions) formed in the distillation (for example, atmospheric distillation and / or vacuum distillation) are referred to herein as distillation effluents.

In other words, the present invention proposes in an advantageous

Embodiment before, the separation insert, such as conventional crude oil streams also, together with the second crude oil stream initially in an atmospheric

To process distillation. In atmospheric distillation, the products of the steam cracking process, such as ethylene and other light ones, go

Hydrocarbons, in the top stream of the distillation column over. 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 the present invention, therefore, the oil column conventionally used in a steam cracking process and in a conventional

Refinery process used distillation column for atmospheric distillation functionally merged. 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 a water wash can be used, in which, if necessary, the naphtha still present in a corresponding stream in liquid form is deposited. 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 other in the column for atmospheric distillation incurred

Distillation effluents are composed of heavier hydrocarbons, predominantly from the uncleaved crude oil or for quenching

used liquid stream. 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 contained in, for example, 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 may be combined and together or separately, optionally together with

Fresh inserts, the same or different cracking furnaces are supplied. 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 supplied 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 result of the inventive measures the advantage that can be dispensed with an oil column, and that no pyrolysis oil and no

Pyrolysis gasoline incurred as separate products. The conventionally in the Pyrolysis oil and pyrolysis gas passing compounds can be found when using the method according to the invention in the corresponding

Distillation effluents (for example, from atmospheric distillation and vacuum distillation) again.

The process according to the invention can also be configured by recycling all distillation effluents which are not desired as products such that they are no longer used for the production of typical refinery products such as gasoline, diesel, heating oil, etc.

comes. 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 for

Preheating the crude oil stream are used, the vaporized portion 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 distillative separation of the separation insert together with the second

Crude oil is, as explained, advantageously initially at atmospheric pressure and then in vacuo, so that can be used for distillation on known methods of refinery technology and appropriate methods 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.

For example, diverted streams can each be derived by branching off a partial stream, combining with other streams, chemical or physical

Reacting at least some components in corresponding streams, heating, cooling, evaporation, condensation, etc. are formed.

With particular advantage corresponding derived currents through

Hydrocracking be formed. In such methods, the

Destillationsabströme, optionally after further separation and / or treatment, 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 recycle streams may be, in particular, atmospheric hydro (ATO) treated by hydrotreatment and / or hydrocracking, and vacuum gas oil treated by hydrotreatment and / or hydrocracking (Vacuum Gasoil, VGO), ie distillation residues from the

atmospheric distillation or vacuum distillation, act. 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 separation by distillation downstream separation stages, which

For example, compounds such as methane, ethylene, propylene, butadiene and / or aromatics (benzene, toluene and / or xylenes, also summarized as BTX

referred to) and carried out of the plant. The Indian

Vacuum distillation resulting and not further usable vacuum residue and / or the methane formed can be fired to produce energy.

A plant for the production of crude oil products, which is adapted to form a gaseous stream from a first stream of crude oil and to subject the gaseous stream at least in part a vapor cracking process, is also Subject of the present invention. The plant is arranged such that in the steam cracking process a split gas stream is generated which is used to form a separation insert contained in the quench effluent

Hydrocarbons containing one, two, three, four and more carbon atoms and / or hydrocarbons formed from such hydrocarbons, and that at least one furnished for fractional distillation distillation column is provided, which is adapted to the separation insert at least in part to give a Quenchabstroms with a liquid hydrocarbon Ström can be quenched. According to the invention, means are provided which are set up to separate at least part of the quench waste stream together with a second crude oil stream to obtain distillate effluents by distillation.

Such a system has all the means that enable it to carry out a method according to the invention.

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.

Brief description of the drawings

Figure 1 shows a plant for the production of crude oil products according to a

Embodiment of the invention in partial view.

Figure 2 shows a plant for the production of crude oil products according to a

Embodiment of the invention in an expanded view. In the figures, corresponding elements are given identical reference numerals and will not be explained repeatedly. The respectively shown

Plant components simultaneously correspond to steps of a process.

Embodiments of the invention In Figure 1 is a plant for the production of crude oil products according to a

Embodiment of the invention 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. One in the

Vaporization tank 2 vaporizing fraction of the crude oil stream b is passed as stream d after mixing with steam through the radiation zone of the cracking furnace or 1, wherein a cleavage gas e is 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

For example, an atmospheric residue h and an atmospheric gas oil i can be 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 portions, which are substantially 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, the system 100 is illustrated in an expanded view, ie as an expanded section of an overall system 100, and designated as a whole by 200. The installation part shown in FIG. 1, that is to say at least one cracking furnace 1 with the associated devices 2 to 4 and a distillation column 5 equipped with a water scrubber 6 and an associated decanter 7 for fractional atmospheric distillation, is designated by 100.

As illustrated in Figure 2, from an atmospheric residue withdrawn as stream h from the distillation column 5, a vacuum residue p is obtained in a distillation column 8 equipped for vacuum distillation, which is fired in a means 9 and for energy, here with arrow q

can be used.

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 current s can in the

Steam splitting method or in one or more cracking furnaces 1 are returned. The same applies to the above-explained stream i, the atmospheric gas oil, which is treated in a hydrogenation unit 1 1 and then as stream t in the

Steam splitting method can be returned. 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 can be used as power w the

Steam splitting process to be subjected again. 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. Hydrocarbons not recovered as product streams x can be recycled as stream z into the steam cracking process.

Claims

claims

1 . Process for the extraction of crude oil products, in which a first

Crude oil (b) a gaseous stream (d) is formed and the gaseous stream (d) at least partially subjected to a vapor cracking method (1), wherein in the vapor cracking process (1) a cracked gas stream (e) is generated, at least in part to obtain a Quenchabstroms (g) with a liquid

Hydrocarbon ström (f) is quenched, characterized in that at least a portion of Quenchabstroms (g) is used to form a separation insert and that the separation insert together with a second

Crude oil stream (c) is separated by distillation (5, 8) to obtain distillation effluents (h, i, k, p, r), wherein the separation insert is formed in such a way that it contains in the quench effluent (g) hydrocarbons having one, two, contains three, four or more carbon atoms and / or hydrocarbons formed from such hydrocarbons.

A process according to claim 1, wherein the separation insert is formed to contain hydrocarbons contained in the liquid hydrocarbon (f) previously used in the quenching liquid hydrocarbon and / or to contain compounds formed from such hydrocarbons.

3. The method of claim 1 or 2, wherein the distillation effluents (h, i, k, p, r) or derived therefrom streams (s, t, w, z) are at least partially subjected as recycle streams to the steam cracking process (1) ,

4. The method of claim 1, 2 or 3, wherein the by catalytic hydrogenation (1 1) treated atmospheric gas oil (i), by 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.

5. The method according to any one of the preceding claims, wherein the gaseous

Stream (d) by evaporation (2) from the first crude oil stream (b) is formed, wherein a in the evaporation (2) liquid remaining proportion (f) at least to Part for the formation of the liquid used for quenching

Hydrocarbon stream (f) is used.

A process according to any one of the preceding claims, wherein the liquid hydrocarbon stream (f) used for quenching is poor in or free from

Is components that from the Quenchabstrom (g) or one from the

Quenchabstrom (f) formed stream were separated.

7. The method according to any one of the preceding claims, wherein the distillative

Separation (5, 8) of the separation insert together with the second crude oil stream (c) first at atmospheric pressure (5) and then in a vacuum (8).

8. The method according to any one of the preceding claims, wherein at least

a part of the distillation effluents (i, r) at least by catalytic

Hydrogenation (10, 1 1) derived currents (s, t) are formed.

9. The method according to any one of the preceding claims, are obtained in the methane, ethylene, propylene and / or butadiene (x) and / or aromatic compounds (v).

10. The method according to any one of the preceding claims, wherein at least a portion of the distillation effluents (p, y) is fired to produce energy.

1 1. A crude oil product plant (100) adapted to form a gaseous stream (d) from a first crude stream (b) and at least partially subject the gaseous stream (d) to a steam cracking process (1), wherein Steam gap method (1), a gap gas stream (e) can be generated and a quench device (4) is provided for this purpose

is arranged to quench at least part of the cracked gas stream (e) to give a quenching stream (g) with a liquid hydrocarbon stream (f), characterized in that means are provided which are adapted to produce at least part of the quench stream (g) to form a

Use separation insert, which contained in the Quenchabstrom (g)

Hydrocarbons having one, two, three, four or more carbon atoms and / or hydrocarbons formed from such hydrocarbons and in that at least one distillation column (5, 8) equipped for fractional distillation is provided, which is arranged to supply the

Separating separation together with a second crude oil stream (c) to obtain distillation effluents (h, i, k, p, r) by distillation.

12. Plant (100) according to claim 1 1, comprising means, which are adapted to carry out a method according to one of claims 1 to 9.