EP3102655A1 - Procédé de production d'oléfines - Google Patents

Procédé de production d'oléfines

Info

Publication number
EP3102655A1
EP3102655A1 EP15704977.6A EP15704977A EP3102655A1 EP 3102655 A1 EP3102655 A1 EP 3102655A1 EP 15704977 A EP15704977 A EP 15704977A EP 3102655 A1 EP3102655 A1 EP 3102655A1
Authority
EP
European Patent Office
Prior art keywords
separation
product
hydrocarbons
insert
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Withdrawn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
EP15704977.6A
Other languages
German (de)
English (en)
Inventor
Clara DELHOMME-NEUDECKER
Torben HÖFEL
Nicole SCHÖDEL
Heinz Zimmermann
Ernst Haidegger
Gunther KRACKER-SEMLER
Harald SCHMADERER
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 EP3102655A1 publication Critical patent/EP3102655A1/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • 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
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/148—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound
    • C07C7/163—Purification; Separation; Use of additives by treatment giving rise to a chemical modification of at least one compound by hydrogenation
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
    • 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
    • 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
    • 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
    • C10G2400/22—Higher olefins
    • 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 process for the preparation of olefins according to the
  • Short chain olefins such as ethylene and propylene can be prepared by steam cracking
  • Hydrocarbons are prepared, as explained in detail below.
  • An alternative route to such short chain olefins are the so-called oxygenate to olefin (Oxygenates to Olefins, OTO) processes.
  • Oxygenates are oxygen-containing compounds derived from saturated hydrocarbons, in particular ethers and alcohols. Oxygenates are used, for example, as fuel additives for increasing the octane number and as a lead substitute (see D. Barcelö (ed.): Fuel Oxygenates. In: D. Barcelö and AG Kostianoy (ed.): The Handbook of Environmental Chemistry, Vol Heidelberg: Springer, 2007). The addition of oxygenates in fuels causes, among other things, a cleaner combustion in the engine and thus reduces emissions.
  • the corresponding oxygenates are typically ethers and
  • methyl tert-butyl ether engl, methyl tertiary butyl ether
  • TAME tertiary amyl methyl ether
  • TEE tertiary amyl ethyl ether
  • EBE ethyl tertiary butyl ether
  • DIPE diisopropyl ether
  • Alcohols are, for example, methanol, ethanol and tert-butanol (TBA, tertiary butyl alcohol) used.
  • the oxygenates include the dimethyl ether explained below (DME, dimethyl ether).
  • DME dimethyl ether
  • oxygenates are compounds which are at least one covalent to an oxygen atom having bound alkyl group.
  • the at least one alkyl group may have up to five, up to four or up to three carbon atoms.
  • the oxygenates of interest herein have alkyl groups with one or two
  • Carbon atoms especially methyl groups.
  • monohydric alcohols and dialkyl ethers such as methanol and dimethyl ether or
  • oxygenates such as methanol or
  • Dimethyl ether introduced into a reaction zone of a reactor in which a suitable catalyst for the implementation of the oxygenates is provided.
  • the catalyst typically contains a molecular sieve. Under the action of the catalyst, the oxygenates are converted, for example, into ethylene and propylene.
  • the catalysts and reaction conditions used in oxygenate-to-olefin processes are basically known to the person skilled in the art.
  • compound plants for the production of hydrocarbons comprising steam cracking processes and oxygenate-to-olefin processes or corresponding cracking 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 substantial portion of the oxygenates is converted to paraffins and C4plus olefins (see below for designation). 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. Furthermore, C4plus olefins, including diolefins such as butadiene, are typically found here. The compounds obtained in both cases depend on the used inserts and reaction conditions.
  • the cracked gas of a cracking furnace and the effluent of an oxygenate-to-olefin reactor are combined and fractionated in a common separation unit.
  • a C4 fraction may be re-subjected to a steam cracking and / or oxygenate-to-olefin process become.
  • the C4 fraction can be separated into predominantly olefinic and predominantly paraffinic fraction fractions.
  • the separation in a common separation unit does not always prove to be satisfactory, especially when obtained in a corresponding integrated process from the oxygenate-to-olefin process and the steam cracking process gas mixtures with significantly different compositions and / or if an existing facility for Steam columns to a plant part to carry out an oxygenate-to-olefin process to be extended.
  • the present invention proposes a method for
  • hydrocarbon mixtures or hydrocarbon fractions are based on the carbon number of the respectively predominantly or exclusively contained compounds.
  • a "C1 fraction” is a fraction which contains predominantly or exclusively methane (but conventionally under certain circumstances also hydrogen, then also called “Cl minus fraction”).
  • a "C2 fraction” contains predominantly or exclusively ethane, ethylene and / or acetylene.
  • a "C3 fraction” contains predominantly propane, propylene, methyl acetylene and / or propadiene.
  • a “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.
  • 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 90%, 95%, 99%, 99.5%, 99.9%, 99.99 % or 99.999% and “poor” for a content of at most 10%, 5%, 1%, 0.1%, 0.01% or 0.001% on a molar, weight or volume basis.
  • Liquid and gaseous streams may also be enriched or depleted in one or more components as used herein, which terms refer to a corresponding level 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, 5, 1, 5, 2, 5, 10, 100 or 1 000 times its content.
  • a stream comprising "predominantly" one or more components contains at least 50% of these one or more components or is rich in them in the above sense.
  • a liquid or gaseous stream is "derived” from another liquid or gaseous stream (also referred to as the exit stream) if it has at least some components contained in or from the exit stream.
  • a derived in this sense current can from the output current through
  • Tubular reactors carried out their reaction tubes, the so-called coils, individually or in groups at the same or different gap conditions can be operated.
  • Reaction tubes or groups of reaction tubes operated under identical or comparable fission conditions, if appropriate, but also operated under uniform fission conditions are referred to below as "cracking furnaces".
  • a cracking furnace in the language used here is thus a structural unit used for the vapor cracking, which equates to a furnace insert or exposes it to comparable cracking conditions.
  • a steam cracking plant may have one or more cracking furnaces. The present application is used for the characterization of pressures and
  • pressure level and "temperature level”, which is to express that corresponding pressures and temperatures in a corresponding system need not be used in the form of exact pressure or temperature values in order to realize the inventive concept.
  • pressures and temperatures typically range in certain ranges, such as ⁇ 1%, 5%, 10%, 20%, or even 50%
  • Corresponding pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels include unavoidable or expected pressure drops, for example, due to cooling effects.
  • Pressure levels are absolute pressures.
  • the present invention further develops known processes for producing olefins in which gas mixtures produced by a steam cracking process and an oxygenate to olefin process are used as a separation feedstock
  • the present invention thus proposes a process for recovering olefins wherein a first gas mixture produced by a steam cracking process is at least partially used to form a first separation insert containing hydrocarbons of one to five carbon atoms.
  • Trennipponin can in addition to the hydrocarbons with one to five
  • Carbon atoms also contain other hydrocarbons and other compounds. It can also contain predominantly or exclusively the hydrocarbons having one to five carbon atoms.
  • the "formation" of a first separation insert comprises not only the use of the first gas mixture as a whole as the first separation insert; a process according to the invention may also comprise using only part of such a gas mixture, optionally after purification and pretreatment steps. As also explained in detail below, in the formation of the first separation insert part of a
  • Gas mixture produced by an oxygenate-to-olefin process also used to form this first separation insert by reacting with the first
  • Formation of a separation insert may include combining streams used for this purpose upstream or in a separation device.
  • the content of hydrocarbons in the first separation insert depends on the operating conditions of the steam cracking process used and, in particular, on the hydrocarbon feeds subjected to the steam cracking process.
  • light hydrocarbons i.
  • the first separation insert naturally contains a smaller proportion of hydrocarbons having five or more carbon atoms.
  • the first separation insert naturally contains a smaller proportion of hydrocarbons having five or more carbon atoms.
  • first separation product and a second separation product are produced from the first separation insert, which was produced as explained above.
  • the first and second separation products may be generated in a common separation unit, but it is also possible that the first separation product in a first separation unit generates a sequence of separation units and the second separation product downstream of this first separation unit in a second, third, etc. separation unit becomes.
  • the first separation product and the second separation product can be produced at the same or different location in a corresponding separation sequence.
  • the first separation product contains at least the predominant proportion of the hydrocarbons having one and two carbon atoms contained in the first separation insert and the second separation product at least the majority of the hydrocarbons having four and five carbon atoms contained in the first separation insert.
  • the first separation product is, in particular, a gaseous overhead stream of a deethanizer or a depropanizer, as is known from the prior art.
  • the second separation product is obtained, for example, as the bottom product of a corresponding deethanizer or depropanizer in the form of a liquid fraction.
  • a second gas mixture which is produced by an oxygenate-to-olefin process, at least partially used to form a second separation insert.
  • the second separation insert also contains hydrocarbons with one to five
  • the second separation insert can in addition to the
  • Hydrocarbons having one to five carbon atoms also more
  • the first separation insert may contain different proportions of hydrocarbons of different chain lengths.
  • such a separation insert may also contain residual oxygenate which has not been reacted in the oxygenate-to-olefin process.
  • the inventive method can however, also include corresponding oxygenates prior to the formation of the second
  • the third separation product contains at least the predominant proportion of those contained in the second separation insert
  • Separating product contains at least the majority of in the second
  • the formation of the third and fourth separation products takes place separately for the formation of the first and second separation products from the first separation insert.
  • a second deethanizer or a second depropanizer is provided which forms the third separation product as the top product and the fourth separation product as the bottom product.
  • the present invention is now characterized in that the third separation product is also at least partially used to form the first separation insert.
  • the third separation product is completely with that in the
  • the first gas mixture obtained which was optionally treated and purified, combined and subjected to a separation for obtaining the first and the second separation product. Further, at least a portion of the fourth release product and at least a portion of the second release product, a third separation insert is formed and also subjected to a separation.
  • the third separation insert is formed and also subjected to a separation.
  • Separating product such as a C2minus or C3minus fraction, which is formed from an effluent of an oxygenate-to-olefin process, fed to a separation insert, which is formed essentially from an effluent of a steam cracking process.
  • a corresponding C3plus or C4plus fraction of the effluent of the oxygenate-to-olefin process is comparable to a fraction
  • Composition obtained from the first separation insert combined.
  • at least one light fraction (low in C 4 plus hydrocarbons) and at least one heavy fraction (low in C 2min hydrocarbons) are first produced from the effluent of an oxygenate-to-olefin process before the different fractions can be combined at an appropriate point with fractions of a effluent of a steam cracking process.
  • the second separation product may contain at least the majority of the hydrocarbons having three carbon atoms contained in the first separation insert.
  • the fourth separation product contains at least the predominant portion in the second
  • Separating insert contained hydrocarbons with three carbon atoms. This means, in other words, that both the first separation insert and the second separation insert are first processed in a deethanizer.
  • Pressurization does not change to the liquid state, and a top product from the deethanizer are further compressed and separated together with the entire gas mixture obtained in a steam cracker, ie from the steam cracking process.
  • the amount of the top product from the deethanizer depends on the catalyst used (see below). For example, ZSM-5 or a
  • Comparable material used it is a relatively small amount.
  • the "entire gas mixture" from the steam cracker is likewise optionally pretreated, for example dried, freed from condensates etc.
  • the significantly higher amount of C3plus hydrocarbons from the oxygenate-to-olefin process can lead directly to C3plus processing be performed in a common separation sequence.
  • the advantage that can be achieved thereby is that, even with considerable differences in the C 2min / C 3 plus ratio in the gas mixture from the oxygenate-to-olefin process and the gas mixture from the steam cracking process, corresponding plant components can be realized more simply and less expensively.
  • Another advantage is the improved separation: if the obtained from the oxygenate-to-olefin process Gas mixture contains carbon dioxide, this will go into the C2minus fraction, ie the third separation product. The carbon dioxide removal may then be carried out together in this fraction and the entire gaseous mixture obtained from the steam cracking process without having to mix the comparatively large amount of C3plus hydrocarbons of the oxygenate-to-olefin process with the gas mixture from the steam cracking process. The latter could lead to carbon dioxide dissolving in the condensates and can not be separated separately.
  • the third separation product may contain at least the predominant portion of the hydrocarbons having three carbon atoms contained in the second separation insert.
  • the gas mixture from the oxygenate-to-olefin process for example, initially quenched, compacted and optionally dried.
  • the compression must be done only to a relatively low value, for example, 10 to 15 bar. Subsequently, a corresponding separation takes place in the depot stimulator.
  • oxygenates such as dimethyl ether
  • the process according to the invention in the illustrated embodiment opens up the possibility of removing dimethyl ether from the C3-minus stream.
  • the third separation insert can be subjected to different treatment steps in the context of the present invention.
  • the third separating insert is at least part of the fourth separating product and at least part of the second separating product.
  • Treatment include a hydrogenation, in which in the third separation insert contained undesirable compounds such as small amounts of butadiene can be removed.
  • first separation product and the second separation product in a first separation unit and the third separation product and the fourth separation product in a structurally separate from the first separation unit second separation unit are generated.
  • structurally separate is meant that corresponding separation units not with a common
  • Fluid stream which is formed from the first separation insert and the second separation insert to be charged.
  • the separation is initially separate.
  • first separation unit and the second separation unit are identical to each other.
  • the first separation product and the third separation product are each produced using a corresponding distillation column.
  • the process according to the invention does not comprise the separation of butadiene from corresponding fractions prior to the union to the third
  • the first separation insert contains butadiene and this is transferred to a predominant proportion in the second separation product
  • the present invention advantageously comprises removing the butadiene from the latter after the formation of the third separation insert. For this purpose can
  • butadiene extraction and / or (through) hydrogenation are used.
  • the remainder can be conditioned, in
  • the invention can work with different catalysts in the oxygenate-to-olefin process.
  • zeolites such as ZSM-5 or SAPO-34 or functionally comparable materials can be used.
  • the present invention is particularly suitable when ZSM-5 or a comparable material is used, because this comparatively large amounts of long-chain (C3plus-) hydrocarbons and relatively small amounts of shorter-chain (C2minus) hydrocarbons are formed.
  • C3plus- long-chain
  • C2minus shorter-chain
  • the latter can, as explained, separated in a separate deethanizer and further processed together with the entire gas mixture obtained from the steam cracking process.
  • the invention is also suitable for use with SAPO-34 or comparable materials with which relatively short-chain (C 2 -min) hydrocarbons are formed.
  • the invention may be implemented in an olefin recovery plant having means adapted to use, at least in part, a first gas mixture produced by a steam cracking process to form a first separation feed, the hydrocarbons having one to five
  • Means are further adapted to produce from the first separation insert at least a first separation product and a second separation product, wherein the first separation product at least the majority of the hydrocarbons contained in the first separation insert having one and two carbon atoms and the second separation product at least the predominant Contains proportion of the hydrocarbons containing four and five carbon atoms contained in the first separation insert.
  • Such a plant further comprises means adapted to at least partially use a second gas mixture produced by an oxygenate-to-olefin process to form a second separation insert
  • second fluid processing means are further adapted to produce from the second separation insert at least a third separation product and a fourth separation product, wherein the third separation product contains at least the predominant portion of those contained in the second separation insert Hydrocarbons having one and two carbon atoms and the fourth
  • Separating product contains at least the majority of the hydrocarbons containing four and five carbon atoms contained in the second separation insert.
  • a system is characterized by means adapted to use the third separation product also at least partially to form the first separation insert (referred to herein as third fluid processing means), and means adapted therefor from at least a part of the fourth release product and from at least a portion of the second release product to form a third separation insert and to subject this to a separation (referred to here as the fourth fluid processing means).
  • the present invention is also suitable for creating a corresponding plant by converting ("revamp") an existing plant, which is set up only for carrying out a steam cracking process and subsequent separation of the resulting gas mixture.
  • a system to be converted thus has the explained first fluid processing means.
  • the refitting may be accomplished by providing means adapted to effect an oxygenate-to-olefin process, for example, at least one oxygenate-to-olefin reactor, and providing and coupling at least the illustrated second fluid processing means and the illustrated third fluid processing means ,
  • the illustrated fourth fluid processing means may be provided and coupled, but may already be present at least in part for processing a corresponding C4plus fraction from the steam cracking process. In this case, it may be necessary to capacitively expand the fourth fluid processing means.
  • Steam cracking operations for example from naphtha to gaseous feeds such as shale gas containing ethane, result in a proportionate reduction of hydrocarbons having three or more carbon atoms in the gaseous mixture obtained by the steam cracking process.
  • Such a conversion may be desirable because appropriate gas mixtures are available inexpensively, for example in the form of shale gas.
  • the total throughput of a corresponding plant is also in the reduction of hydrocarbons having three or more carbon atoms in the gas mixture obtained by the steam cracking method further by the dimensioning of the present in a corresponding separation sequence separation units for and
  • Fluid processing means, the third fluid processing means and possibly the fourth (possibly already partially existing) fluid processing means this underload can be compensated. If, for example, a parallel oxygenate-to-olefin reactor with separate water wash and compaction and a subsequent C2 / C3 separation is provided, the C3plus can be used for processing
  • Hydrocarbons are used in the existing separating part.
  • Small amounts of a C2 fraction from the oxygenate to olefin process can be further processed in an existing compressor and in the existing separation unit.
  • the resulting C4plus fraction (predominantly from the oxygenate-to-olefin process) can utilize the still available capacity of the cracking furnaces by recycling them.
  • the invention can also be applied to the capacity expansion of a plant exclusively or predominantly steam-cracked naphtha without an increase in the amount of naphtha processed by the steam cracking process, or else in a reduction of the amount of naphtha processed by the steam cracking process.
  • a C4plus recycle from an oxygenate-to-olefin reactor supplemented during the conversion can also be fed to the existing cracking furnaces and a corresponding amount of naphtha can be saved.
  • the capacities in the process groups of the steam cracking process would not change significantly except for the C3plus part.
  • the increase in capacity would be due to the additional propylene from the oxygenate to olefin part.
  • the C3plus part can be enlarged comparatively easily in this case.
  • the invention may also offer particular advantages when an addition of a steam cracking process with predominantly C2 / C3 use, ie a so-called gas cracker, to an oxygenate-to-olefin process is carried out.
  • a steam cracking process with predominantly C2 / C3 use ie a so-called gas cracker
  • the comparatively low C2 content from the oxygenate-to-olefin process can be co-processed in the existing components to carry out the steam cracking process.
  • Gasfeedmenge be slightly reduced so that the capacities of the crude gas compressor and the cold part for the C2minus hydrocarbons from the oxygenate-to-olefin process and the products from the gas ovens and the C4plus furnaces sufficient.
  • Propylene / ethylene ratio is relatively high.
  • a conventional conversion measure eg feed conversion from naphtha to gas
  • conversion measures appear attractive, which result in an increase of the propylene / ethylene ratio.
  • the present invention enables a corresponding conversion.
  • FIG. 1 shows a method according to an embodiment of the invention in FIG.
  • FIG. 2 shows a method according to an embodiment of the invention in FIG.
  • FIG. 3 shows a method according to an embodiment of the invention in FIG.
  • FIG. 4 shows a method according to an embodiment of the invention in FIG.
  • FIG. 1 schematically shows a method according to an embodiment of the invention in the form of a flow chart.
  • the method is designated 100 as a whole.
  • the process 100 comprises the parallel implementation of a steam cracking process 1 and an oxygenate-to-olefin process 2.
  • a plant in which the process 100 is implemented has corresponding means, ie at least one cracking furnace and at least one oxygenate-to-olefin Reactor.
  • the steam cracking process 1 operates using one or more
  • Feed streams a which can be fed to one or more operated at the same or different conditions cracking furnaces, as explained above.
  • the streams a may comprise fresh feeds or any recycle streams from a corresponding process 100. Recycling streams can, for example
  • Fresh inserts can be provided, for example, in gaseous and / or liquid form, for example in the form of natural gas and / or naphtha.
  • a crude gas stream b is obtained, which can be supplied to one or more treatment steps.
  • an oil fractionation and / or a quench takes place in one
  • Process step 3 process steam can be generated in the
  • Steam splitting method 1 can be returned (not shown).
  • a gas stream c obtained in process step 3 becomes, for example, a
  • a process step 4 can also be supplemented by an acid gas removal 5 (for example, by diverting a gas stream between two compressor stages from the process step 4 to the sour gas removal 5 and subsequently fed back), forming corresponding streams d.
  • a C2-minus current e can also be at a pressure level of, for example, 20 bar
  • medium-pressure C2minus current which consists of a corresponding
  • Gas mixture of an oxygenate-to-olefin process 2 is formed can be used, as explained below.
  • the combined use of the stream c and the C 2 minus stream e from the oxygenate-to-olefin process 2 ensures that a corresponding pretreatment must be carried out only once and not separately again for the comparatively small amounts of C 2 -minus hydrocarbons from one Oxygenate-to-olefin process 2.
  • An obtained from the process step 4, in particular compressed and partially liquefied and dried stream f is subjected in the example shown as a separation Entethanizer Colour 6 in which a C2minus fraction g at a pressure level of, for example, 35 bar (high-pressure C2minus-current) and a C3plus- Fraction h is obtained. Further processing of the C3plus fraction h will be explained below.
  • the C2minus fraction g is subjected, for example, to a hydrogenation step 7, in which, in particular, acylene is hydrogenated to ethylene.
  • a stream i treated further in this way is subsequently subjected, for example, to a demethanizer step 8, in which methane CH4 and hydrogen H2 are separated off.
  • the ethylene C2H4 is taken from the process 100 as a product, the ethane C2H6 can for example be recycled to the steam cracking process 1. at
  • a method 100 according to the invention can also work with recirculated streams in the steam splitting method 1.
  • the C3plus stream h from the deethanizer step 6 is subjected to a depropanizer step 10.
  • the depropanizer step 10 can also be supplied with a C3plus fraction I, which is obtained from a gas mixture from the oxygenate-to-olefin process 2, as explained below. This allows another common
  • a common (third) separation insert is formed and separated in the depropanizer step 10.
  • Formation of a separation insert may, as mentioned, comprise combining streams used for this purpose upstream or in a corresponding separation device.
  • the currents h and I can also be upstream of the depropanizer step 10
  • a C3 fraction m is formed, which can be processed in one or more further process steps.
  • the C3 fraction m is subjected to a hydrogenation step 11, so that contained methylacetylene and propadiene is converted to propylene.
  • the thus processed stream now denoted by n, for example, is subjected to a C3 T renn suits 12 in which essentially propylene C3H6 and propane C3H8 are formed.
  • the propylene C3H6 can be taken from a corresponding process 100 as a product, the propane C3H8, however, in the
  • C9plus stream essentially a C4 to C8 stream and a C9plus stream (without short names) are formed.
  • the C9plus stream is withdrawn from process 100, while the C4 to C8 stream, in turn, can be recycled to steam cracking process 1.
  • the oxygenate-to-olefin process 2 is particularly useful for the reaction of
  • methanol and other oxygenates can be implemented.
  • Corresponding oxygenates are supplied as stream q to one or more reactors and converted to an olefin-containing gas mixture r.
  • the gas mixture r which contains at least or predominantly hydrocarbons having one to five carbon atoms, becomes a
  • Post-treatment step 15 for example, a water quench and a removal of oxygenates.
  • Correspondingly obtained water is withdrawn as stream s, a freed from oxygenates stream t is fed to a step 16 explained below.
  • Recovered oxygenates can be recycled as stream j to the oxygenate to olefin process 2.
  • the stream t is compressed and possibly pre-cooled.
  • a condensation of condensable components of the current t is optionally dried and subjected as stream u liquid to a deethanizer step 17, in which from the stream u the already mentioned C 2 minus fraction e and the C 3 plus fraction I are formed.
  • Depropanizer step 10 on the other hand supplied.
  • the condensation step 16 non-condensable constituents of the stream t are combined as stream v with the C 2minus stream e.
  • FIG. 2 shows a corresponding variant of a device according to the invention
  • a C3minus current is supplied as a current y and the method step 13 together with the C4plus current o a C4plus current z and no longer the process step 10, a C3plus current I is supplied.
  • a common (third) separation insert is formed from the currents z and o and separated in the depropanizer step 10.
  • the streams z and o can also be brought together upstream of the method step 13 and subjected to method step 13 as a collective stream.
  • at least one oxygenate stream q is fed to the oxygenate-to-olefin process 2 and further processed, as described above, in each case while the streams r to v are obtained.
  • the condensate in the form of the current u becomes one here
  • Depropanizer step 18 supplied in which a C3 minus current w is obtained. This is combined with stream v and subjected to an oxygenate removal step 19. An oxygenate stream x separated in the oxygenate removal step 19 is combined with the stream j and subjected to the oxygenate-to-olefin process 2 again. A C3 minus stream y freed from oxygenates is then subjected to process step 4 already explained. As already explained, a C4plus current z obtained in the depropanizer step 18 is supplied to method step 13.
  • FIG. 3 illustrates a method according to the invention in a generalized form.
  • the elements used here correspond to those which have been explained with reference to FIGS. 1 and 2, but in particular a series of separation steps are summarized in FIG. 3 as blocks 1 10 to 140.
  • the steam cracking process 1 the already explained feed streams a are supplied.
  • An obtained stream b is subjected to the aftertreatment steps 3 and 4 of FIGS. 1 and 2 already mentioned, which are summarized here as block 10.
  • the combined aftertreatment steps 110 for example, a water stream, oil and gasoline (illustrated as arrow 1 1 1) deducted.
  • the correspondingly purified gas mixture g is subjected to a common separation step 120, in which, for example, the method steps 4 to 12 of FIGS. 1 and 2 are integrated.
  • Hydrogen H2, methane CH4, carbon dioxide CO2, ethylene C2H4, ethane C2H6, propylene C3H6, propane C3H8 and C4plus hydrocarbons o are formed in the common separation step 120, as described in detail above with reference to FIGS. 1 and 2.
  • Ethane C2 H6 and propane C3H8 are recycled to the steam cracking process 1 as explained above.
  • the C4plus stream o is subjected to a previously described in detail separation 130, which includes, for example, the process steps 13 and 14 shown in Figures 1 and 2, wherein products 131 can be removed and recycle fractions 132 are returned to the steam cracking process 1.
  • the oxygenate-to-olefin process 2 operates using the already mentioned oxygenate stream q.
  • An obtained stream r is subjected to a pre-treatment, densification and pre-separation 140, for example as described with reference to FIGS.
  • At least one stream 141 is formed which may include, for example, water, oxygenates and gasoline. A recycle is possible.
  • the process comprises pre-separation into one or more Fractions 142 which are low in C4plus hydrocarbons and one or more Fractions 143 which are low in C 2 -minus hydrocarbons.
  • these fractions each contain C3 hydrocarbons (as in detail to the currents e and I of Figure 1 and the
  • Conversion of an existing plant in which the steam cracking process 1 and the treatment and separation steps 110, 120 and 130 are already implemented includes providing plant components implementing the oxygenate-to-olefin process 2 and the downstream separation 140.
  • FIG. 4 illustrates a method according to a further embodiment of the invention, which consists in particular of a subsequent extension of a plant in which a steam cracking process 1 is implemented, to corresponding steps of a Oxygenate-to-olefin process results.
  • the steps 150 to 170 of the oxygenate-to-olefin process shown here correspond, for example, to the so-called Lurgi process.
  • FIG. 4 corresponds to the exceptions
  • An oxygenate-to-olefin process designated 150 here, becomes here
  • a gas mixture R is obtained, which is subjected in particular to an after-treatment step such as, for example, a water quench and to a compression and, if appropriate, drying 160.
  • an after-treatment step such as, for example, a water quench and to a compression and, if appropriate, drying 160.
  • One or more compressed and dried, optionally partially liquefied streams S are subjected to product separation 170.
  • Streams such as liquefied natural gas and gasoline, illustrated here as stream J may be at least partially re-subjected to the oxygenate-to-olefin process 150 and are subjected to deplapanizer step 10 other than C3plus stream L.
  • propylene C3H6 is further formed, which can be discharged from a corresponding process.
  • production of propylene C3H6 at this point can also be dispensed with by passing a separate C3 fraction to depropanizer step 10.
  • the recycle streams J and the stream L would no longer contain propane C3H8 (C4plus).
  • a C 2 minus stream E generated in step 170 is fed to process step 4 and no longer, as illustrated by the dashed arrow, returned to the oxygenate-to-olefin process 150 or, as is not shown separately, from the plant dissipated.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé (100) de production d'oléfines, dans lequel un premier mélange de gaz (b), qui est produit par un procédé de craquage à la vapeur (1), est utilisé au moins partiellement pour former un première charge de séparation (f) qui contient des hydrocarbures ayant un à cinq atomes de carbone, et à partir de laquelle sont générés au moins un premier produit de séparation (g) et un second produit de séparation (h, o), le premier produit de séparation (g) contenant au moins la majeure partie des hydrocarbures à un et deux atomes de carbone qui sont contenus dans la première charge de séparation (f) et le second produit de séparation (h, o) contenant la majeure partie des hydrocarbures à quatre et cinq atomes de carbone qui sont contenus dans la première charge de séparation (f), et dans lequel un second mélange de gaz (R), qui est produit par un procédé (2) de conversion d'un produit oxygéné en oléfines, est utilisé au moins partiellement pour former une seconde charge de séparation (t) qui contient des hydrocarbures ayant un à cinq atomes de carbone et à partir de laquelle sont générés au moins des troisième (e, y), et quatrième (l, z) produits de séparation, le troisième produit de séparation (e, y) contenant au moins la majeure partie des hydrocarbures à un et deux atomes de carbone qui sont contenus dans la seconde charge de séparation (t) et le quatrième produit de séparation (l, z) contenant la majeure partie des hydrocarbures à quatre et cinq atomes de carbone qui sont contenus dans la seconde charge de séparation (t). Le troisième produit de séparation (e, y) est également utilisé au moins partiellement pour former la première charge de séparation (f) et une troisième charge de séparation (h, l) (o, z), qui est soumise à une séparation (14), est formée à partir d'au moins une partie des quatrième (l, z) et deuxième (h, o) produits de séparation.
EP15704977.6A 2014-02-06 2015-02-06 Procédé de production d'oléfines Withdrawn EP3102655A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102014001652 2014-02-06
EP14001241 2014-04-03
PCT/EP2015/052514 WO2015118108A1 (fr) 2014-02-06 2015-02-06 Procédé de production d'oléfines

Publications (1)

Publication Number Publication Date
EP3102655A1 true EP3102655A1 (fr) 2016-12-14

Family

ID=52477780

Family Applications (1)

Application Number Title Priority Date Filing Date
EP15704977.6A Withdrawn EP3102655A1 (fr) 2014-02-06 2015-02-06 Procédé de production d'oléfines

Country Status (11)

Country Link
US (1) US20160347688A1 (fr)
EP (1) EP3102655A1 (fr)
JP (1) JP2017508038A (fr)
CN (1) CN105980530A (fr)
AU (1) AU2015214225A1 (fr)
BR (1) BR112016018098A2 (fr)
CA (1) CA2937458A1 (fr)
EA (1) EA201691475A1 (fr)
MX (1) MX2016010183A (fr)
PH (1) PH12016501437A1 (fr)
WO (1) WO2015118108A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11078435B2 (en) 2019-05-05 2021-08-03 Uop Llc Process for cracking an olefinic feed comprising diolefins and monoolefins

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101081998B (zh) * 2006-05-31 2010-05-12 中国石油化工股份有限公司 一种c4馏分的加氢方法
CN101343562B (zh) * 2007-07-09 2011-09-21 中国石油化工股份有限公司 一种汽油加氢脱硫、降烯烃方法
RU2560185C2 (ru) 2009-11-10 2015-08-20 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Способ и интегрированная система для приготовления низшего олефинового продукта
WO2011057978A2 (fr) * 2009-11-10 2011-05-19 Shell Internationale Research Maatschappij B.V. Procédé pour la préparation d'un produit oléfinique inférieur
US20120041243A1 (en) * 2010-08-10 2012-02-16 Uop Llc Integration of a methanol-to-olefin reaction system with a hydrocarbon pyrolysis system
CN103649021B (zh) * 2011-07-07 2016-06-01 英尼奥斯欧洲股份公司 利用从蒸汽裂化向醇脱水过程的传热制备烯烃的方法和设备
US20130172627A1 (en) 2011-12-28 2013-07-04 Shell Oil Company Process for preparing lower olefins
CN104520256A (zh) 2012-07-05 2015-04-15 国际壳牌研究有限公司 用于制备烯烃的集成方法

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO2015118108A1 *

Also Published As

Publication number Publication date
US20160347688A1 (en) 2016-12-01
MX2016010183A (es) 2016-11-15
CA2937458A1 (fr) 2015-08-13
PH12016501437A1 (en) 2017-02-06
WO2015118108A1 (fr) 2015-08-13
AU2015214225A1 (en) 2016-08-25
EA201691475A1 (ru) 2017-02-28
BR112016018098A2 (pt) 2017-08-08
CN105980530A (zh) 2016-09-28
JP2017508038A (ja) 2017-03-23

Similar Documents

Publication Publication Date Title
DE102005048931B4 (de) Verfahren und Anlage zur Herstellung von C2-C4-Olefinen aus Methanol und/oder Dimethylether
DE102005003109B4 (de) Verfahren zur Herstellung von synthetischen Kraftstoffen aus Oxigenaten
WO2009039948A2 (fr) Procédé et installation pour la production d'hydrocarbures
EP3191434A1 (fr) Procédé et installation pour la production d'hydrocarbures
DE10217863A1 (de) Verfahren und Vorrichtung zur Olefinherstellung
EP3312261B1 (fr) Procédé de séparation d'un mélange d'hydrocarbures
WO2019012062A1 (fr) Procédé et installation de production de propylène par combinaison d'une déshydrogénation de propane et d'un procédé de vapocraquage comprenant des étapes de séparation préalable dans les deux procédés pour l'élimination partielle d'hydrogène et de méthane
DE10217866A1 (de) Verfahren und Vorrichtung zur Olefinherstellung
WO2015118125A1 (fr) Procédé et installation de production d'oléfines
EP3652137B1 (fr) Procédé et installation de fabrication de propylène par combinaison de déshydrogénation de propane et procédé de vapocraquage avec recyclage de propane au procédé de vapocraquage
EP3510008B1 (fr) Procédé et installation de production de benzène
EP3102655A1 (fr) Procédé de production d'oléfines
EP3041916B1 (fr) Procédé de production d'hydrocarbures
EP0555301B1 (fr) Procede et installation de production de carburants liquides et de matieres premieres chimiques
EP3191433A1 (fr) Procédé et installation pour la production d'hydrocarbures
EP3041917B1 (fr) Procédé de production d'hydrocarbures
WO2015140300A1 (fr) Procédé et dispositif de production d'oléfines
DE102013014866A1 (de) Verfahren und Anlage zur Erzeugung von Kohlenwasserstoffprodukten
DE102013014867A1 (de) Verfahren und Anlage zur Erzeugung von Kohlenwasserstoffprodukten
DE102015208943A1 (de) Verfahren und Anlage zur Bearbeitung eines Stoffgemischs
DE102013014802A1 (de) Verfahren und Anlage zur Erzeugung von Kohlenwasserstoffprodukten

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20160906

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

RIN1 Information on inventor provided before grant (corrected)

Inventor name: ZIMMERMANN, HEINZ

Inventor name: HOEFEL, TORBEN

Inventor name: SCHOEDEL,NICOLE

Inventor name: SCHMADERER, HARALD

Inventor name: KRACKER-SEMLER, GUNTHER

Inventor name: HAIDEGGER, ERNST

Inventor name: DELHOMME-NEUDECKER, CLARA

DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20170715