EP3137578B1 - Procédé de production de produits de pétrole brut - Google Patents

Procédé de production de produits de pétrole brut Download PDF

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Publication number
EP3137578B1
EP3137578B1 EP15721173.1A EP15721173A EP3137578B1 EP 3137578 B1 EP3137578 B1 EP 3137578B1 EP 15721173 A EP15721173 A EP 15721173A EP 3137578 B1 EP3137578 B1 EP 3137578B1
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Prior art keywords
stream
crude oil
quench
streams
hydrocarbons
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EP15721173.1A
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German (de)
English (en)
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EP3137578A1 (fr
Inventor
Heinz Zimmermann
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Linde GmbH
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Linde GmbH
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Priority claimed from DE102014006327.5A external-priority patent/DE102014006327A1/de
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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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • 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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C10G70/041—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by distillation
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • 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
    • C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
    • C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/002—Cooling of cracked gases
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4006—Temperature
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics

Definitions

  • the invention relates to a process for the production of crude oil products according to the preamble of claim 1.
  • 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.
  • atmospheric distillation fractional distillation at atmospheric pressure
  • 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.
  • a steam 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
  • 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.
  • TLE transfer line exchanger
  • the first cooling step ie the cooling of the quenching gas with cooling water, for example in the quench cooler
  • quenching the cooling of the quenching gas with cooling water
  • the second cooling step may therefore also be referred to as oil quench for better distinctness.
  • quench effluent The stream formed by combining the cracked gas stream with the liquid stream used for quenching is referred to herein as quench effluent.
  • 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.
  • 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.
  • 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.
  • 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 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 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.
  • 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 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 according to an advantageous embodiment of the method, in particular unchanged a common distillative separation together with the second crude oil stream.
  • 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 suitably equipped distillation column along 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.
  • the Quenchabstrom or the separation insert can be transferred together with the used for quenching liquid hydrocarbon stream in a corresponding distillation column, in which the usual crude oil fractions are obtained.
  • 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 in the invention.
  • the inventive method can therefore be realized with significantly less expenditure on equipment than a method of the prior art, as it 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.
  • 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 Quenchölniklauf, 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. 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.
  • 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 Quenchniklauf used, as it is known from conventional methods.
  • 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.
  • a lower portion of the lower portion of the cracked gas stream is fed and sent towards the Quenchöl.
  • 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.
  • pyrolysis gasoline is abandoned, which is separated in a downstream water quench and also partially circulated.
  • 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.
  • 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 exactly come into contact with the cleavage gas stream. 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 cracked 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.
  • 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.
  • 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 .
  • the temperature difference between the temperature values is significantly higher.
  • the current obtained is therefore still at a very high temperature, which requires a further quench before further processing.
  • the temperature of the quenching 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.
  • the Quenchabstrom is obtained by the advantageous quenching with the liquid hydrocarbon stream at a temperature which is in a temperature range of 0 to 250 ° C, in particular from 50 to 200 ° C or from 50 to 150 ° C, ie at a temperature , which is also achieved in a conventional oil column, and the direct further processing of Quenchabstroms allows.
  • the cracked gas stream, before it is quenched with the liquid hydrocarbon stream has already been cooled to a temperature which is 50 to 200 ° C, for example 100 to 150 ° C, above the temperature of the quench effluent and, for example, the typical inlet temperatures in 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.
  • further quench oil in particular an oil circuit.
  • 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.
  • 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.
  • the separation insert is formed from at least part of the quench effluent, which is separated by distillation together with the second crude oil stream 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 present invention proposes, in an advantageous embodiment, to process the separation insert, such as conventional crude oil streams, together with the second crude oil stream initially in an 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.
  • the classical sections of the crude oil stream can be produced in this distillation column.
  • 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.
  • 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 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.
  • atmospheric gas oil English: Atmospheric Gas Oil, AGO
  • 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.
  • 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 conventionally in the Pyrolysis oil and the pyrolysis of passing compounds are found when using the method according to the invention in the corresponding distillation effluents (for example, from the 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 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.
  • appropriate treatment such as hydrotreats or (mild) hydrocracking
  • 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.
  • 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 stream 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 treating the distillation effluents can be used.
  • distillation effluents or streams derived therefrom may also be at least partially subjected to the steam cracking process.
  • 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.
  • corresponding derived streams can be formed by hydrocracking.
  • the distillation effluents if appropriate after prior further separation and / or treatment, are partially or fully catalytically hydrogenated and at least partially cracked.
  • 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 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.
  • a plant for the production of crude oil products may be adapted to form a gaseous stream from a first stream of crude oil and to subject the gaseous stream at least in part to a steam cracking process.
  • the attachment may be arranged to produce in the vapor cracking process a cracked gas stream used to form a separation insert containing hydrocarbons having one, two, three, four and more carbon atoms and / or hydrocarbons formed in the quench effluent, and in that at least one distillation column equipped for fractional distillation is provided, which is arranged to be able to quench the separation insert at least partly with a liquid hydrocarbon stream to obtain a quench effluent stream.
  • Means may be provided which are arranged to distillatively separate at least part of the quench effluent together with a second crude oil stream to obtain distillation effluents.
  • Such a system can have all means that enable it to carry out a method according to the invention.
  • 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.
  • 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.
  • a stream k is withdrawn containing light products from the cracking furnace (s) 1 and the crude oil stream c.
  • a water scrubber 6 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.
  • 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.
  • a 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).
  • 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.
  • 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 correspondingly processed stream s can be returned to the steam cracking process or into one or more cracking furnaces 1.
  • the atmospheric gas oil which can be treated in a hydrogenation unit 11 and subsequently recycled as stream t into the steam cracking process.
  • 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. Hydrocarbons not recovered as product streams x can be recycled as stream z into the steam cracking process.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (10)

  1. Procédé pour la production de produits à base de pétrole brut, dans lequel on forme, à partir d'un premier flux de pétrole brut (b), un flux gazeux (d) et le flux gazeux (d) est soumis au moins en partie à un procédé de dissociation (1) à la vapeur, un flux gazeux dissocié (e) étant obtenu dans le procédé de dissociation (1) à la vapeur, qui est au moins en partie refroidi brusquement à l'aide d'un flux hydrocarboné liquide (f) avec obtention d'un effluent refroidi brusquement (g), caractérisé en ce qu'au moins une partie de l'effluent refroidi brusquement (g) est utilisé pour la formation d'une charge de séparation et en ce que la charge de séparation est séparée par distillation (5, 8), conjointement avec un deuxième flux de pétrole brut (c), avec obtention d'effluents de distillation (h, i, k, p, r), la charge de séparation étant formée de manière telle qu'elle contient des hydrocarbures contenus dans l'effluent de refroidissement brusque (g) présentant un, deux, trois, quatre atomes de carbone et plus et/ou des hydrocarbures formés à partir de ces hydrocarbures.
  2. Procédé selon la revendication 1, dans lequel la charge de séparation est formée en ce qu'elle contient des hydrocarbures qui étaient contenus au préalable dans le flux hydrocarboné liquide (f) utilisé pour le refroidissement brusque et/ou en ce qu'il contient des composés formés à partir de ces hydrocarbures.
  3. Procédé selon la revendication 1 ou 2, dans lequel les effluents de distillation (h, i, k, p, r) ou des flux dérivés de ceux-ci (s, t, w, z) sont au moins en partie soumis au procédé de dissociation (1) à la vapeur en tant que flux de recyclage.
  4. Procédé selon la revendication 1, 2 ou 3, dans lequel on utilise du gazole (i) atmosphérique traité par hydrogénation catalytique (11), du gazole (r) sous vide traité par hydrogénation catalytique, des hydrocarbures saturés (z) comprenant deux à quatre atomes de carbone et/ou des hydrocarbures (w) comprenant cinq à huit atomes de carbone comme flux de recyclage.
  5. Procédé selon l'une quelconque des revendications précédentes, dans lequel le flux gazeux (d) est formé par évaporation (2) à partir du premier flux de pétrole brut (b), une proportion (f) qui reste liquide lors de l'évaporation (2) étant utilisée au moins en partie pour la formation du flux hydrocarboné liquide (f) utilisé pour le refroidissement brusque.
  6. Procédé selon l'une quelconque des revendications précédentes, dans lequel le flux hydrocarboné liquide (f) utilisé pour le refroidissement brusque est pauvre en ou exempt de composants qui ont été séparés de l'effluent de refroidissement brusque (g) ou d'un flux formé à partir de l'effluent de refroidissement brusque (f).
  7. Procédé selon l'une quelconque des revendications précédentes, dans lequel la séparation par distillation (5, 8) de la charge de séparation conjointement avec le deuxième flux de pétrole brut (c) a d'abord lieu à la pression atmosphérique (5) et ensuite sous vide (8).
  8. Procédé selon l'une quelconque des revendications précédentes, dans lequel on forme des flux (s, t) dérivés à partir d'au moins une partie des effluents de distillation (i, r), au moins par hydrogénation catalytique (10, 11).
  9. Procédé selon l'une quelconque des revendications précédentes, dans lequel du méthane, de l'éthylène, du propylène et/ou du butadiène (x) et/ou des composés aromatiques (v) sont obtenus.
  10. Procédé selon l'une quelconque des revendications précédentes, dans lequel au moins une partie des effluents de distillation (p, y) sont brûlés pour la production d'énergie.
EP15721173.1A 2014-04-30 2015-04-28 Procédé de production de produits de pétrole brut Active EP3137578B1 (fr)

Applications Claiming Priority (3)

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DE102014006327.5A DE102014006327A1 (de) 2014-04-30 2014-04-30 Verfahren und Anlage zur Gewinnung von Rohölprodukten
EP14003150 2014-09-11
PCT/EP2015/059250 WO2015165921A1 (fr) 2014-04-30 2015-04-28 Procédé et installation pour l'obtention de produits pétroliers

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EP3137578B1 true EP3137578B1 (fr) 2018-06-20

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US (1) US10000711B2 (fr)
EP (1) EP3137578B1 (fr)
JP (1) JP2017516893A (fr)
KR (1) KR20160146766A (fr)
CN (1) CN106232779B (fr)
AU (1) AU2015254695A1 (fr)
BR (1) BR112016025290A2 (fr)
HU (1) HUE039134T2 (fr)
PH (1) PH12016501940A1 (fr)
RU (1) RU2016142702A (fr)
WO (1) WO2015165921A1 (fr)

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Publication number Priority date Publication date Assignee Title
US7374664B2 (en) 2005-09-02 2008-05-20 Equistar Chemicals, Lp Olefin production utilizing whole crude oil feedstock
US7550642B2 (en) * 2006-10-20 2009-06-23 Equistar Chemicals, Lp Olefin production utilizing whole crude oil/condensate feedstock with enhanced distillate production
US8118996B2 (en) * 2007-03-09 2012-02-21 Exxonmobil Chemical Patents Inc. Apparatus and process for cracking hydrocarbonaceous feed utilizing a pre-quenching oil containing crackable components
US20090050523A1 (en) * 2007-08-20 2009-02-26 Halsey Richard B Olefin production utilizing whole crude oil/condensate feedstock and selective hydrocracking
US8105479B2 (en) 2009-06-18 2012-01-31 Exxonmobil Chemical Patents Inc. Process and apparatus for upgrading steam cracker tar-containing effluent using steam

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Publication number Publication date
WO2015165921A1 (fr) 2015-11-05
HUE039134T2 (hu) 2018-12-28
CN106232779A (zh) 2016-12-14
US10000711B2 (en) 2018-06-19
BR112016025290A2 (pt) 2017-08-15
CN106232779B (zh) 2018-09-21
AU2015254695A1 (en) 2016-10-20
US20170058215A1 (en) 2017-03-02
PH12016501940A1 (en) 2017-01-09
JP2017516893A (ja) 2017-06-22
RU2016142702A (ru) 2018-05-30
KR20160146766A (ko) 2016-12-21
RU2016142702A3 (fr) 2018-08-29
EP3137578A1 (fr) 2017-03-08

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