EP3191434A1 - Procédé et installation pour la production d'hydrocarbures - Google Patents

Procédé et installation pour la production d'hydrocarbures

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Publication number
EP3191434A1
EP3191434A1 EP15763314.0A EP15763314A EP3191434A1 EP 3191434 A1 EP3191434 A1 EP 3191434A1 EP 15763314 A EP15763314 A EP 15763314A EP 3191434 A1 EP3191434 A1 EP 3191434A1
Authority
EP
European Patent Office
Prior art keywords
stream
hydrocarbons
butene
isobutene
carbon atoms
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP15763314.0A
Other languages
German (de)
English (en)
Inventor
Torben HÖFEL
Helmut Fritz
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Publication of EP3191434A1 publication Critical patent/EP3191434A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/04—Thermal processes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
    • C07C41/01—Preparation of ethers
    • C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
    • C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/23—Rearrangement of carbon-to-carbon unsaturated bonds
    • C07C5/25—Migration of carbon-to-carbon double bonds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • C10G3/42—Catalytic treatment
    • 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
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • the invention relates to a method and a plant for the production of
  • Short-chain olefins such as ethylene and propylene can be prepared by steam cracking.
  • oxygenate to olefin Oxygenates to Olefins, OTO
  • oxygenates such as methanol or dimethyl ether are introduced into a reaction zone of a reactor in which a catalyst suitable for reacting the oxygenates is provided.
  • a catalyst suitable for reacting the oxygenates is provided.
  • the oxygenates are converted to ethylene and propylene.
  • the catalysts and reaction conditions used in oxygenate-to-olefin processes are known in principle to the person skilled in the art.
  • Oxygenate-to-olefin processes can be carried out with different catalysts
  • zeolites such as ZSM-5 or SAPO-34 or functionally comparable materials can be used.
  • ZSM-5 or a comparable material comparatively large ones form
  • compound plants for the production of hydrocarbons, the steam cracking process and oxygenate-to-olefin process or corresponding slit furnaces and reactors are known and described for example in WO 201 1/057975 A2 or US 2013/0172627 A1.
  • Such integrated processes are advantageous, for example, because in the oxygenate-to-olefin process, typically, only the desired short-chain olefins are typically not formed. A significant portion of the oxygenates is converted to paraffins and C4plus olefins. At the same time, not all of the furnace charge is split into short-chain olefins during steam cracking. In particular, unreacted paraffins may be present in the cracking gas of corresponding cracking furnaces. Further, typically C4plus olefins are found here, including diolefins such as butadiene. The compounds obtained are in both cases according to the used
  • a C4 fraction obtained here may, for example, after hydrogenation or separation of butadiene, again be subjected to a steam cracking and / or an oxygenate-to-olefin process.
  • the C4 fraction can be separated into predominantly olefinic and predominantly paraffinic fraction fractions.
  • the present invention is not limited to oxygenate-to-olefin processes, but can in principle be used with any catalytic process, in particular with catalytic processes in which the zeolites explained above are used as catalysts.
  • catalytic processes in which the zeolites explained above are used as catalysts.
  • other oxygenates for example other alcohols and / or ethers, can be used as an insert in corresponding catalytic processes.
  • olefinic components such as a mixture of different unsaturated C4 hydrocarbons
  • olefinic components can be used in corresponding catalytic processes.
  • OCP English Olefins Cracking Process
  • Different uses can be carried out in the context of the present invention in the same reactor or in different reactors.
  • an oxygenate-to-olefin process and another reactor may use an olefin cracking process be performed.
  • both processes, but possibly also a combined process have the goal of producing from one or more operations a product rich in propylene and possibly ethylene.
  • the illustrated catalytic processes which are distinguished in particular by the fact that the mentioned zeolites are used as catalysts and furthermore one or more catalyzer feed streams containing oxygenates and / or olefins are used, are thus carried out in a catalytic unit containing one or more corresponding reactors can have.
  • US 4,197,185 A proposes a process for the production of butane and high octane gasoline from a C4 olefin cut derived from a steam splitter unit.
  • the process comprises polymerizing at least 90% of the isobutene in the C4 olefin cut mainly to dimers and trimers, the resulting
  • This object is achieved by a method and a plant for the production of
  • Liquid and gaseous streams may be rich or poor in one or more components as used herein, with “rich” for a content of at least 75%, 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” for a content of at most 25%, 10%, 5%, 1%, 0.1% or 0.01% may be on a molar, weight or volume basis.
  • the term “predominantly” may correspond to the definition of "rich” just mentioned, but in particular denotes a content of more than 90%. Liquid and gaseous streams can be found here
  • the language used may also be enriched or depleted of one or more components, these terms referring to a corresponding content in a starting mixture from which the liquid or gaseous stream was obtained.
  • the liquid or gaseous stream is "enriched” if it is at least 1, 1-fold, 1, 5-fold, 2-fold, 5-fold, 10-fold, 100-fold or 1,000-fold content, "depleted” if it contains not more than 0,9 times, 0, 5 times, 0,1 times, 0,01 times or 0,001 times the content of a corresponding component, relative to the starting mixture.
  • a liquid or gaseous stream is "derived” from, or “formed from, another liquid or gaseous stream (also referred to as the exit stream) if it has at least some components contained or derived from the exit stream.
  • a derived or formed in this sense current can from the output stream in particular by separating or branching a substream or one or more components, enriching or depleting of one or more components, chemical or physical
  • C1 fraction is a fraction which contains predominantly or exclusively methane (and conventionally also possibly hydrogen, then also called “Cl minus fraction”).
  • C2 fraction contains predominantly or exclusively ethane, ethylene and / or acetylene.
  • a "C3 fraction” contains predominantly or exclusively propane, propylene, methyl acetylene and / or propadiene.
  • C4 fraction contains predominantly or exclusively butane, butene, butadiene and / or butyne, it being possible for the respective isomers to be present in different proportions, depending on the source of the C4 fraction.
  • C5 fraction contains predominantly or exclusively butane, butene, butadiene and / or butyne, it being possible for the respective isomers to be present in different proportions, depending on the source of the C4 fraction.
  • C5 fraction and the higher fractions.
  • Hydrocarbons having two or more and a "C 2 -minus fraction" predominantly or exclusively hydrocarbons having one and two carbon atoms.
  • Oxygenates are typically understood as meaning ethers and alcohols.
  • methyl-ie-f-butyl ether MTBE, Engl., Methyl tertiary butyl ether
  • MTBE methyl-ie-f-butyl ether
  • TAME tertiary amyl methyl ether
  • TAEE ie / f-amyl ethyl ether
  • EBE ethyl-ie F-butyl ether
  • DIPE diisopropyl ether
  • oxygenates include, in particular, dimethyl ether (DME, dimethyl ether).
  • DME dimethyl ether
  • oxygenates are compounds which have at least one alkyl group covalently bonded to an oxygen atom.
  • the at least one alkyl group can be up to five, have up to four or up to three carbon atoms.
  • the oxygenates of interest in the present invention are
  • Alkyl groups having one or two carbon atoms are methyl groups.
  • they are monohydric alcohols and dialkyl ethers such as methanol and dimethyl ether or corresponding mixtures.
  • Coils so-called coils
  • Reaction tubes can be operated at different clearance conditions. Operated under the same or similar fission conditions
  • Reaction tubes or groups of reaction tubes, if appropriate, but also operated under uniform fission conditions tubular reactors in total, are also referred to as "cracking furnaces".
  • a cracking furnace is used in here
  • Steam splitter unit used in the context of the present invention may comprise one or more such cracking furnaces.
  • the same also applies, as already mentioned, for the catalytic unit used in the context of the present invention in which different reactors equipped with identical or different catalysts can be charged with the same or different feed streams and operated under the same or different reaction conditions.
  • vapor column feed streams here refers to one or more liquid and / or gaseous streams which are fed to one or more cracking furnaces. Also, streams obtained by a corresponding steam cracking process, as explained below, may be recycled to one or more cracking furnaces and reused as vapor column feed streams.
  • Suitable steam column feed streams are a variety of hydrocarbons and hydrocarbon mixtures of ethane to gas oil up to a boiling point of typically 600 ° C.
  • a steam column feed stream may comprise only so-called "fresh use”, ie an insert which is provided externally and, for example, made out of the system one or more petroleum fractions, natural gas and / or natural gas condensates is obtained.
  • a steam column feed stream may additionally or exclusively comprise one or more so-called “recycle streams”, ie streams which are generated in the plant itself and returned to a corresponding cracking furnace.
  • a steam column feed stream can therefore also consist of a mixture of one or more fresh feeds with one or more recycle streams.
  • the steam column feed stream is at least partially reacted in the respective cracking furnace and leaves the cracking furnace as so-called "raw gas", the
  • post-treatment steps include first treating the raw gas, for example, by quenching, cooling and drying, whereby a "cracking gas" is obtained.
  • the raw gas is already referred to as cracking gas.
  • steam cracking product stream is used for this purpose.
  • Catalytic units fed feed streams which are referred to herein as “catalytic feed streams”.
  • the catalytic feed stream (s) are reacted in the catalytic unit in one or more reactors into one or more product streams, referred to herein as “catalyst product streams”.
  • the mentioned "cracking conditions" in a cracking furnace include, inter alia, the partial pressure of the furnace insert, which can be influenced by the addition of different amounts of steam and the pressure set in the cracking furnace, the residence time in Cracking furnace as well as the temperatures and temperature profiles used in this.
  • the furnace geometry and furnace design also plays a role.
  • the term "cracking severity" has been used to characterize the fission conditions.
  • the gap resolution can be described by the ratio of propylene to ethylene (P / E) or by the ratio of methane to propylene (M / P) in the cracked gas on a weight basis (kg / kg).
  • the conversion or conversion of each considered component of the furnace insert can be specified as a measure of the gap sharpness.
  • a description of the resolution of the gap via the reaction of key components such as n-butane and isobutane is well suited.
  • the present invention combines the above-explained measures for the use of hydrocarbons such as four or more carbon atoms from a corresponding catalytic process in an optimized manner, so that overall efficient utilization with maximum added value and low internal
  • the present invention is directed to a process for producing hydrocarbons comprising, in a catalytic unit using one or more catalytic streams containing oxygenates and / or olefins, an n-butane, isobutane, 1-butene, 2-butene, Isobutene and hydrocarbons containing more than four and / or less than four carbon atoms
  • the catalytic unit comprises, as explained above, one or more reactors charged with one or more feed streams, referred to herein as catalysis feed streams.
  • the present invention is useful in oxygenate-to-olefin processes and / or the so-called olefin cracking process.
  • the one or the other in a corresponding
  • Catalysis unit used reactors are preferably zeolites Catalysts on. As explained, these catalysts may be in particular of the SAPO or ZSM type.
  • the catalytic unit used in the context of the present invention is thus set up for a corresponding catalytic process.
  • the method contemplates generating a vapor gap product stream in a vapor column unit using one or more vapor column feed streams.
  • the steam cracking process used in the context of the present invention can be carried out using the same or different steam cracking conditions in one or more cracking furnaces, as basically known. For details, reference is made to the above explanations.
  • the steam column feed streams used in steam cracking can be mildly cleaved to increase the yield of value products.
  • Harsher cracking conditions can be used in particular to achieve the highest possible conversion.
  • the present invention proposes to first generate a C4 cut from the catalytic product stream obtained in a corresponding catalytic unit, namely by the aforementioned removal of the predominant
  • Invention also depleted of isobutene, i. selectively on the previously included unsaturated branched C4 hydrocarbon, but not on all unsaturated hydrocarbons. Also, isobutane can still be included.
  • corresponding hydrocarbons it can be encompassed by that, such as As explained in the introduction, at least 75% or more of such hydrocarbons are removed.
  • corresponding hydrocarbons are substantially completely removed, ie in particular at least 90 or 95%, and if appropriate also at least 99% or more.
  • the remainder i. the stream which is at least 5 mole percent, more preferably at least 10 mole percent, at least 20 mole percent or at least 30 mole percent, and most preferably at most 90 mole percent, at most 80 mole percent, at most 70 mole percent, at most 60 mole percent, at most 50 mole percent or at most 40 mole percent, 1-butene and / or 2-butene, from which, however, further
  • Components can be separated, or one or more streams formed therefrom, is or are supplied in the form of one or more streams of steam column unit used, where it is the same or different
  • Cleavage conditions are split in one or more cracking furnaces. As explained in more detail below, from the vapor gap product stream, which in a corresponding
  • Catalytic product stream or a C4 cut generated therefrom are combined.
  • the method proposed in the context of the present invention is particularly efficient, since here the isobutene unsuitable for the vapor cracking is removed, but all other components are largely removed as vapor column feed stream or
  • Catalysis unit be recycled.
  • the method according to the invention provides that initially the major part of the hydrocarbons having more than four and / or less than four carbon atoms is removed while leaving a C4 substream, and
  • the removal of the predominant part of the isobutene comprises the at least partial reaction of the isobutene and the separation of at least part of the reaction product formed thereby.
  • Appropriate measures facilitate the removal of isobutene considerably, so that can be dispensed with elaborate separation devices.
  • it is suitable for the at least partially
  • Catalysis unit returned and further implemented there.
  • At least a portion of a stream remaining after removal of most of the isobutene containing the above-mentioned amounts of 1-butene and / or 2-butene may be used as the one or more of the vapor column feed streams, if no further Separation of components is desired. Because a corresponding stream only contains little or substantially no isobutene, the steam cracking process can be adapted flexibly to the respective products to be obtained.
  • distillative removal has the advantage that isobutene can be obtained directly, ie not as a corresponding reaction product.
  • the boiling point of isobutene at atmospheric pressure is -6.9 ° C, that of 1-butene at -6.47 ° C.
  • a distillative separation is practically not possible.
  • the boiling point of 2-butene is significantly higher than this, namely at 3.7 ° C for c / ' s-2-butene and at 0.9 ° C for frans-2-butene.
  • butane and 2-butene-containing stream may also be advantageous to form a predominantly butane and 2-butene-containing stream from at least a portion of a stream remaining after removal of most of the isobutene and to use it as the vapor column feed stream or one of the vapor column feed streams.
  • removal of components other than the one mentioned is also carried out here.
  • the components mentioned, namely n-butane and 2-butene, are particularly suitable as
  • Steam gap feed stream or one of the steam column feed streams may be provided in the context of the present invention to form a stream containing predominantly n-butane and 2-butene from an isobutene, isobutane and, if appropriate, 1-butene and n-butane and 2-butene-containing stream, and to feed this to the steam splitting unit.
  • a remaining stream containing isobutene, isobutane and optionally 1-butene may be subjected to a distillation process in which the isobutane is separated off. This can, as mentioned, be treated in the vapor column unit.
  • a corresponding vapor split product stream contains hydrocarbons having four carbon atoms, including butadiene, and hydrocarbons having more than four and / or less than four carbon atoms.
  • a composition of a corresponding stream can, as mentioned, by adjusting the used
  • Hydrocarbons having more than four and / or less than four carbon atoms are separated from the vapor split product stream to give a butadiene-lean residual stream containing predominantly hydrocarbons having four carbon atoms.
  • This allows the extensive recovery of butadiene and the Return of corresponding other compounds.
  • at least part of the butadiene-lean residual stream is combined with at least part of the above-explained C4 substream.
  • a plant according to the invention is set up for the production of hydrocarbons.
  • It comprises at least one catalytic unit adapted to use, using one or more catalytic streams containing oxygenates and / or olefins, an n-butane, isobutane, 1-butene, 2-butene, isobutene and hydrocarbons of greater than 4 and / or less to produce four carbon atoms containing catalytic product stream.
  • Such a plant comprises a steam-splitting unit which is adapted to use one or more steam-gap feed streams
  • means are provided in a corresponding system which are adapted to remove at least the majority of the hydrocarbons having more than four and / or less than four carbon atoms and the isobutene from the catalytic product stream or a part thereof, whereby a stream is formed, the at least 5 mole percent,
  • FIG. 1 shows a system according to an embodiment of the invention in
  • FIG. 2 shows a plant according to an embodiment of the invention in FIG.
  • FIG. 3 shows a plant according to an embodiment of the invention in FIG.
  • FIG. 1 a system according to an embodiment of the invention is shown schematically simplified and designated 100 in total.
  • the catalytic unit 1 are here one or more, oxygenates and / or olefins containing catalytic feed streams, here designated a, fed.
  • the catalytic unit 1 may comprise one or more reactors operated with a zeolite catalyst.
  • the catalytic unit can additionally be charged with further streams, in this case the stream e, as explained below.
  • a catalytic product stream b is generated in the illustrated example. This is fed to a separation unit 3, in which from the
  • Catalysis product stream b is a stream c depleted in hydrocarbons having more than four and / or less than four carbon atoms or enriched in hydrocarbons having four carbon atoms, ie a C4 stream.
  • the thereby separated streams here denoted by y and z, for example Hydrocarbons with five or more or hydrocarbons with three and fewer carbon atoms or similar other fractions include.
  • Such streams can also be processed in a corresponding facility and / or obtained as products.
  • the C4 stream c is fed to a reaction unit 4 in which isobutene contained in the C4 stream c is reacted, for example, with methanol, which is supplied in the form of a stream d, to give methyl ie / f-butyl ether.
  • Methyl ie / f-butyl ether or another reaction product with another compound supplied in the form of stream d can be withdrawn as stream e.
  • at least a portion of corresponding products may be executed as stream f from the plant. The remaining portion of the stream e or the entire stream e can be fed again into the catalytic unit 1 and thus used as a recycle stream.
  • a C4 stream freed from isobutene in this manner is fed to the steam splitting unit 2 and processed therein in one or more cracking furnaces, optionally also together with further streams which are passed into identical or different cracking furnaces. It will be a
  • Steam gap product stream s containing, as explained, hydrocarbons having four carbon atoms, including butadiene, and hydrocarbons having more than four and / or less than four carbon atoms.
  • This stream here denoted by s, is fed to a further separation unit 5, in which initially a stream v is obtained with removal of hydrocarbons having more than four and / or less than four carbon atoms, as illustrated here with the streams t and u. which contains predominantly hydrocarbons having four carbon atoms, including butadiene.
  • the current v is in the example shown in a
  • a remaining, butadienarmer residual stream here denoted by x, can be combined with the previously discussed C4 partial stream c and fed into the reaction unit 4.
  • the vapor splitter feed stream (s) may be hydrogenated in advance. In this way, a propylene or ethylene yield can be further increased.
  • a (partial) hydrogenation and / or hydroisomerization, which may also be provided, can also be used to hydrogenate any polyunsaturated components still present and to react 1-butene to 2-butene, which in turn promotes butadiene production. All procedures have
  • FIG. 2 schematically shows a plant according to a further embodiment of the invention, designated overall by 200.
  • Reaction unit 4 provided for the implementation of the isobutene, but optionally, as illustrated in the form of a dashed block 7, an isomerization unit.
  • the separation unit denoted by 3 in FIG. 1 is denoted by x, but may be identical.
  • the isomerization unit 7 is particularly adapted to isomerize 1-butene contained in stream c (and stream x) to 2-butene to facilitate subsequent distillation in a distillation unit 8, as discussed above.
  • the isomerization unit 7 is set up in particular for hydroisomerization. Due to the isomerization in the
  • Isomerization unit 7 are preferably used in the distillation unit 8
  • a stream i is obtained in the distillation unit 8, which contains predominantly isobutene and isobutane, but not the 1-butene which otherwise also passes into a corresponding fraction or the stream i, since this was isomerized in the isomerization unit 7. If no corresponding isomerization, 1-butene also passes into the current i.
  • Another stream obtained in the distillation unit 8, here denoted by n essentially contains butane and 2-butene, which are used as a vapor column feed stream and fed into the vapor splitter unit 2.
  • the stream i is optionally treated in a further distillation unit 9, where an isobutene stream k or, if the stream i still contains 1-butene, a stream k containing isobutene and 1-butene is produced in the stream i the catalytic unit can be returned.
  • a current I obtained in the further distillation unit 9 essentially contains isobutane and is referred to as
  • the isobutene can be returned to the catalytic unit in the form of the flow k and / or be discharged from a corresponding system in the form of the flow m.
  • the isobutene can be returned to the catalytic unit in the form of the flow k and / or be discharged from a corresponding system in the form of the flow m.
  • FIG. 3 schematically shows a system according to a further embodiment of the invention, designated overall by 300.
  • the plant 300 of FIG. 3 corresponds, up to the reaction unit 4, essentially to the plant 100 according to FIG. 1.
  • a partial stream o is obtained from the isobutene-depleted C4 hydrocarbon stream g, which essentially comprises isobutane and 1-butene. This is fed to a further distillation unit, which is also designated here by 9.
  • a stream p containing essentially 1-butene and a stream q containing essentially isobutane are produced from the stream o.
  • the current q can, like a current r, in the
  • Distillation unit 8 is generated and contains predominantly butane and 2-butene, are fed as Dampfspaltganstrom the steam splitter unit 2.
  • the steam splitter unit 2 For the currents s to x and the units 5 and 6, reference is made to the above explanations to FIG. Overall, in all of the systems shown 100 to 300
  • Separation units 3 or x and 5 are further processed together.
  • paraffins especially ethane and propane, can be recycled to the vapor splitter unit 2.
  • Fractionation can take place and certain fractions can be recycled to the catalytic unit 1 and / or, if appropriate after hydrogenation, into the vapor splitter unit 2. It should be emphasized that in certain process variants also other fractions can be processed, for example fractions which also contain C5, C6 and higher hydrocarbons. Further embodiments of the present invention could also provide fully hydrogenating the separated isobutene fraction, which in particular still contains 1-butene and isobutane, and also supplying it to a vapor-splitting unit 2, if any
  • a steam-splitting unit 2 can in all cases also be supplied with further operations, for example naphtha and / or ethane or propane.

Abstract

L'invention concerne un procédé pour produire des hydrocarbures, comprenant les étapes consistant à produire, dans une unité de catalyse (1), au moyen d'un ou de plusieurs flux de départ de catalyse (a) contenant des oxygénates et/ou des oléfines, un flux de produit de catalyse (b) contenant du n-butane, de l'isobutane, du 1-butène, du 2-butène, de l'isobutène et des hydrocarbures comportant plus de quatre et/ou moins de quatre atomes de carbone, puis à produire, dans une unité de séparation en phase vapeur (2), au moyen d'un ou plusieurs flux de départ de séparation en phase vapeur (g, n, l, r), un flux de produit de séparation en phase vapeur (s). Selon l'invention, au moins la majeure partie des hydrocarbures comportant plus de quatre et/ou moins de quatre atomes de carbone et de l'isobutène est éliminée du flux de produit de catayse (b) ou d'une partie de ce dernier, ce qui forme un flux (g, n) contenant au moins 5 % en moles d'1-butène et/ou de 2-butène, et ce flux (g, n) ou un ou plusieurs flux (l, r) dérivés de ce dernier sont utilisés comme flux de départ de séparation en phase vapeur (g, n, l, r). L'invention porte aussi sur une installation correspondante (100, 200, 300).
EP15763314.0A 2014-09-11 2015-09-11 Procédé et installation pour la production d'hydrocarbures Withdrawn EP3191434A1 (fr)

Applications Claiming Priority (2)

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EP14184458.9A EP2995600A1 (fr) 2014-09-11 2014-09-11 Procédé et dispositif pour la production d'hydrocarbures
PCT/EP2015/070888 WO2016038209A1 (fr) 2014-09-11 2015-09-11 Procédé et installation pour la production d'hydrocarbures

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EP3191434A1 true EP3191434A1 (fr) 2017-07-19

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CA (1) CA2959446A1 (fr)
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SG11202008332SA (en) 2018-03-19 2020-09-29 Sabic Global Technologies Bv Method of producing a fuel additive
KR20200133360A (ko) 2018-03-19 2020-11-27 사빅 글로벌 테크놀러지스 비.브이. 연료 첨가제 제조 방법
CN112020547A (zh) 2018-05-07 2020-12-01 沙特基础工业全球技术有限公司 生产燃料添加剂的方法
EP3793969A1 (fr) 2018-05-18 2021-03-24 SABIC Global Technologies B.V. Procédé de production d'un additif de carburant par une unité d'hydratation
US11339332B2 (en) 2020-01-29 2022-05-24 Saudi Arabian Oil Company Systems and processes integrating fluidized catalytic cracking with metathesis for producing olefins
US11572516B2 (en) 2020-03-26 2023-02-07 Saudi Arabian Oil Company Systems and processes integrating steam cracking with dual catalyst metathesis for producing olefins
US11845705B2 (en) 2021-08-17 2023-12-19 Saudi Arabian Oil Company Processes integrating hydrocarbon cracking with metathesis for producing propene

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FR2401122A1 (fr) * 1977-08-26 1979-03-23 Inst Francais Du Petrole Procede pour la conversion des coupes c4 olefiniques de vapocraquage en isooctane et en butane
AU2010318050B2 (en) 2009-11-10 2013-12-12 Shell Internationale Research Maatschappij B.V. Process and integrated system for the preparation of a lower olefin product
US20130172627A1 (en) 2011-12-28 2013-07-04 Shell Oil Company Process for preparing lower olefins

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WO2016038209A1 (fr) 2016-03-17
EP2995600A1 (fr) 2016-03-16
CA2959446A1 (fr) 2016-03-17
CN106715363A (zh) 2017-05-24
US20170253540A1 (en) 2017-09-07
RU2017107754A (ru) 2018-10-11

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