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
  • 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
  • C10G3/54—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed
  • C10G3/55—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds
  • C10G3/57—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids characterised by the catalytic bed with moving solid particles, e.g. moving beds according to the fluidised bed technique
• • 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

Definitions

• the invention relates to a process and a plant for the production of olefins according to the preambles of the independent claims.
• 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
• MTBE engl, methyl tertiary butyl ether
• TAME tert-amyl methyl ether
• TEE tertiary amyl methyl ether
• TAEE 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 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.
• 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.
• the catalyst typically contains a molecular sieve. Under the action of the catalyst, the oxygenates are converted into, for example, ethylene and propylene.
• the catalysts and reaction conditions used in oxygenate-to-olefin processes are basically known to the person skilled in the art.
• 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.
• ZSM-5 or a comparable material comparatively large amounts of longer-chain (C3plus) hydrocarbons and comparatively small amounts of shorter-chain (C2minus) hydrocarbons are formed.
• SAPO-34 or similar materials as well
• oxygenate-to-olefin process is therefore understood below to mean both a process in which one or more of the oxygenates mentioned (not only methanol and / or dimethyl ether) are converted by catalytic conversion at least partially to olefins, but also a method in which a corresponding reactor is charged with a predominantly olefinic use. Also several, loaded with different uses and / or under
• 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 / 172627 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.
• An essential part of the oxygenates is in
• Paraffins and C4plus olefins (see below for description). 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 an oxygenate-to-olefin process.
• the C4 fraction can be found in predominantly olefinic and predominantly
• the present invention proposes a process and a plant for the production of olefins with the characteristics of the independent
• 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.
• C2plus fraction contains predominantly or exclusively hydrocarbons having two or more and a “C2minus fraction” predominantly or exclusively hydrocarbons having one or two carbon atoms and hydrogen.
• Tubular reactors carried out, the reaction tubes, the so-called coils, operated individually or in groups at the same or different gap conditions can be.
• 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.
• Oven furnaces belonging to the total furnace generally have independent radiation zones and a common convection zone as well as a common smoke outlet. In these cases, each furnace cell can be operated with its own gap conditions. Each furnace cell is thus a structural unit used for vapor columns, which are similar or comparable to a furnace insert
• Cleavage conditions exposes and is therefore referred to here as cracking furnace.
• the total furnace then has several corresponding units or, in other words, several cracking furnaces. If there is only one furnace cell, this is the splitting unit and thus the cracking furnace.
• Cracking furnaces can be combined into groups, which are supplied, for example, with the same furnace insert. The fission conditions within a furnace group are usually set the same or similar.
• furnace insert 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 furnace feed. As a furnace insert is a variety of
• a furnace insert may consist of a so-called "fresh use”, ie an insert which is provided externally and obtained, for example, from one or more mineral oil fractions, natural gas and / or natural gas condensates.
• a furnace insert can also consist of one or more so-called “recycle streams”, ie streams that are generated in the plant itself and returned to a corresponding cracking furnace.
• a furnace insert may also consist of a mixture of one or more fresh feeds with one or more recycle streams.
• the furnace insert is at least partially reacted in the respective cracking furnace and leaves the cracking furnace as a so-called "raw gas", which can be subjected to post-treatment steps.
• Such aftertreatment steps comprise first a treatment of the raw gas, for example by quenching, compacting,
• cracking gas Liquefying, cooling and drying, whereby a so-called "cracking gas" is obtained.
• the raw gas is already referred to as cracking gas.
• 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 set pressure in the cracking furnace, the residence time in the cracking furnace and the temperatures and temperature profiles used therein.
• the furnace geometry and furnace design also plays a role. For production of
• a cracking furnace is typically operated at a furnace inlet temperature of 500 to 680 ⁇ and at a furnace exit temperature of 77 5 to 875 ⁇ .
• the "furnace exit temperature” is the temperature of a gas stream at the end of one or more reaction tubes. Typically, this is the maximum temperature to which the corresponding gas stream is heated.
• the pressure used, also measured at the end of one or more reaction tubes, is typically 165 to 225 kPa.
• the furnace insert is admixed with steam in a ratio of typically 0.25 to 0.85 kg of steam per kg of dry feed. The values used are of the furnace used and the desired
• Hydrocarbons the slit-sharpness on the ratio of propylene to Ethylene (P / E) or as the ratio of methane to propylene (M / P) in the fission gas on a weight basis (kg / kg).
• P / E propylene to Ethylene
• M / P methane to propylene
• the P / E and M / P ratios are directly dependent on the temperature, but, in contrast to the real temperature, can be measured more accurately in or at the outlet of a cracking furnace and, for example, used as a controlled variable in a control process.
• the conversion or conversion of a respective considered component of the furnace insert can be specified as a measure of the gap resolution.
• the splitting or cleavage conditions are "sharp" when more than 92% of n-butane is reacted in a corresponding fraction. At even sharper cleavage conditions, n-butane may also be converted to greater than 93%, 94% or 95%. A conversion of n-butane to 100% typically does not occur.
• the upper limit of the "sharp" splitting or cleavage conditions is therefore for example 99%, 98%, 97% or 96% conversion of n-butane.
• Cleavage conditions are "mild" when n-butane is converted to less than 92%. With less than 91%, less than 90%, less than 89%, less than 88% or less than 87% conversion of n-butane, increasingly milder splitting or cleavage conditions are present. With less than 86% conversion of n-butane, the gap-sharpening or cleavage conditions are referred to herein as "very mild”. Very mild splitting or cleavage conditions also include, for example, a conversion of n-butane to less than 85%, 80% or 75% and more than 50% or 60%.
• the mentioned gap sharpening or cleavage conditions depend in particular on the above-explained furnace outlet temperature at the end of the reaction tube or slit furnaces used in each case. The higher this is, the “sharper”, the lower, the “milder” the gap sharpening or gap conditions.
• the key component in this case n-butane, is in each case one kiln outlet temperature and the respective percentage conversions of the other components in use connected.
• This furnace outlet temperature is in turn dependent, among other things, on the cracking furnace.
• the offset between the respective percentage conversions depends on a number of other factors.
• the present invention is based on a method known so far
• olefins in which by means of a steam cracking process, a first gas mixture and by means of an oxygenate-to-olefin process, a second gas mixture is generated, wherein the first gas mixture and the second gas mixture each contain at least hydrocarbons having one to four carbon atoms.
• the first and / or the second gas mixture may also contain hydrocarbons having more than four carbon atoms and / or hydrogen, as well as others
• gas mixtures are not completely subjected to a common separation process in the context of the present invention, as is known, for example, from the aforementioned WO 201 1/057975 A2 and / or US 2013/172627 A1.
• a first fraction is formed from the first gas mixture (which is produced by means of the vapor cracking method), which fraction comprises at least the predominant part of the particles previously contained in the first gas mixture
• Gas mixture (which is produced by the oxygenate-to-olefin process) to form a second fraction, at least the majority of the in the second
• Gas mixture previously contained hydrocarbons containing four carbon atoms.
• the separation of the two gas mixtures thus takes place at least partially separately from one another, which offers the advantage of being able to specifically treat the products obtained therefrom selectively with different compositions of the first and second gas mixture.
• a "predominant" part is understood to mean at least 75%, 80%, 85%, 90%, 99% or more.
• the C4- and optionally longer-chain hydrocarbons from the second gas mixture without further treatment, ie separation or chemical reaction are returned to the steam cracking process and subjected there mild cleavage conditions.
• those in the second gas mixture i. in a product stream of an oxygenate-to-olefin process, contained hydrocarbons having four and possibly more carbon atoms cleaved under mild cleavage conditions, residual hydrocarbons, especially those from the first
• gas mixture i.e., from the steam cracking process
• the second fraction is advantageously low in hydrocarbons of one to three carbon atoms. It thus contains hydrocarbons having one to three carbon atoms preferably only at most 20%, 10%, 5%, 1%, 0.1%, 0.01% or 0.001% on a molar, weight or volume basis.
• the hydrocarbons which are particularly suitable for this purpose which are contained in particular in the second gas mixture, mildly or even very mildly, so that here the particular advantages of mild or very mild cleavage conditions mentioned above , to adjust.
• the second gas mixture contains a comparatively high proportion of butenes, which can be converted into the desired product butadiene under the mild cleavage conditions.
• the invention enables this selective treatment of the hydrocarbons, which are contained in particular in the second gas mixture, in a particularly simple manner. Unlike in US 2013/0172627 A1, for example, previously pooled fractions need not be separated from each other in a laborious manner. There will be no additional media, for example for extractive distillation, and no comparatively expensive devices needed.
• the cracking conditions to which the hydrocarbons contained in the second fraction and previously in the second gas mixture are subjected in the steam cracking process are preferably mild to very mild. This is possible because there are no interfering components that are converted into undesirable products during vapor cracking and thus could, for example, interfere with subsequent separation or the steam cracking process itself.
• Fissile conditions to which the hydrocarbons contained in the second fraction and previously in the second gas mixture are subjected in the steam cracking process result in less than 91%, 90%, 89%, 88%, 87%, 85%, 80% or 75 % and more than 50% or 60% of the contained n-butane is reacted.
• first fraction contained or formed from these hydrocarbons may be at least partially subjected to the steam cracking process, if a Diolefinentfernung takes place.
• sharp or at least normal cleavage conditions are preferably used to process these hydrocarbons.
• fission conditions that result in more than 92%, 93%, 94%, or 95% of the contained n-butane being reacted.
• Hydrocarbons may be formed, for example, hydrogenated or otherwise structurally modified by known methods compounds. In other words, it is possible to include those contained in the first fraction
• hydrocarbons in one or more steps, for example, to get to compounds that can be processed particularly advantageous in a corresponding steam cracking process.
• Ethane and propane from the first and / or the second gas mixture can be converted, for example, in a so-called gas cracker, so a cracking furnace designed to split C2 and C3 hydrocarbons, by steam columns. In this case, again different gap conditions can be used. It is also possible, at least partially, to subject the oxygenates contained in or formed from the second gas mixture and / or the second fraction to the oxygenate-to-olefin process. Corresponding oxygenates can thus be recycled into the oxygenate-to-olefin process.
• the invention makes it possible to carry out a selective process procedure which can be tuned to the respective desired products, and thus proves to be particularly flexible compared to known processes.
• At least two or three operated at different gap conditions cracking furnaces or furnace cells are used.
• At least one cracking furnace is provided, which operates at the aforementioned mild cracking conditions and the said second fraction, that is, the fraction containing the majority of the contained in the second gas mixture hydrocarbons having four carbon atoms, and from the oxygenate to olefin Process originates, is supplied.
• this first fraction is preferably low in hydrocarbons having three and fewer carbon atoms.
• the second fraction is therefore formed from the second gas mixture with removal of at least a major part of the hydrocarbons having not more than three carbon atoms previously contained in the second gas mixture, for example using a depropanizer or a corresponding separation sequence.
• the method according to the invention is also advantageous if the steam cracking process operates completely without fresh feed, ie the steam cracking process is subjected exclusively to hydrocarbons contained in the first gas mixture and / or in the second gas mixture or formed therefrom. A corresponding method thus only requires an oxygenate feed, a separate provision of a separate fresh feed for the steam cracking process is not required.
• a plant for the production of olefins is also an object of the present invention.
• a corresponding plant has means which are adapted to a first gas mixture by means of a steam cracking process and by means of a
• Oxygenate-to-olefin process to produce a second gas mixture, so that the first gas mixture and the second gas mixture each contain hydrocarbons having one to four carbon atoms.
• further means are provided which are adapted to form from the first gas mixture a first fraction which contains at least the predominant part of the four carbon atoms previously contained in the first gas mixture to form a second fraction of the second gas mixture, the at least the majority of the previously contained in the second gas mixture hydrocarbons containing four carbon atoms, and those contained in the second fraction and previously in the second gas mixture
• FIG. 1 shows process steps of a process for the production of olefins
• 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 method 100 includes performing a steam cracking process 1 and an oxygenate-to-olefin process 2 in parallel.
• a plant in which the process 100 is implemented has corresponding means, i. here several cracking furnaces and at least one oxygenate-to-olefin reactor.
• the steam cracking process 1 operates in the example shown using a plurality of feed streams which can be fed to a plurality of cracking furnaces operated at different cracking conditions.
• three cracking furnaces 1 a, 1 b and 1 c are illustrated.
• the cracking furnace 1 a is operated at sharp or normal gap conditions, and this furnace is supplied with a stream a, for example a fresh feed and / or a recycle stream.
• the stream illustrated with a can also be formed from a plurality of streams.
• the method according to the invention can also be the exclusive use of recycle streams in the steam cracking process 1 include.
• Recycled streams may be, for example, ethane and / or propane streams and / or streams of hydrocarbons having four to eight carbon atoms
• Fresh inserts may be provided in gaseous and / or liquid form, for example in the form of natural gas and / or naphtha.
• the cracking furnace 1 b is operated in the example shown at mild gap conditions and charged at least with a current y.
• the stream y is produced as a fraction of a gas mixture s formed by means of the oxygenate-to-olefin process 2 (referred to here as second fraction or second gas mixture).
• the stream y contains at least the hydrocarbons contained in the second gas mixture s with four
• Carbon atoms possibly also longer-chain hydrocarbons (see below).
• the core of the present invention is the recycling of these and preferably only these hydrocarbons for mild cleavage in the cracking furnace 1b.
• a further cracking furnace 1 c is illustrated, which is referred to as a so-called gas cracker and can be charged with suitable feed streams, for example ethane C 2 H 6, as illustrated here.
• suitable feed streams for example ethane C 2 H 6, as illustrated here.
• Other gaseous inserts are also suitable.
• the cracking furnace 1 c can be operated at yet different gap conditions than the cracking furnaces 1 a and 1 b.
• a total of a gas mixture b is obtained, which is referred to here as the first gas mixture and one or more
• a gas stream c obtained in process step 3 becomes, for example, a
• a process step 4 can, with the formation of corresponding currents d, also be supplemented by an acid gas removal 5, in which, for example, a gas stream between two compressor stages is derived from the process step 4 for acid gas removal 5 and subsequently fed back.
• a C3-minus current e which is formed from a corresponding second gas mixture s of an oxygenate-to-olefin process 2 can also be used, as explained below.
• the combined use of the stream c and the C3minus stream e from the oxygenate-to-olefin process 2 ensures that a corresponding pretreatment need only be carried out once and not separately again for the comparatively small amounts of C3minus hydrocarbons from one Oxygenate to Olefin Method 2. This is optional.
• 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 insert a Deethanizer Colour 6, in which a C2minus fraction g and a C3plus fraction h is obtained. Further processing of the C3plus fraction h will be explained below.
• the C2-minus fraction g is subjected, for example, to a hydrogenation step 7, in which in particular acetylene 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.
• a thus freed from methane and hydrogen stream k, which contains substantially still hydrocarbons having two carbon atoms, is subjected to a C2-T renn Colour 9 (for example, in a so-called C2 splitter), formed in the substantially ethylene C2H4 and ethane C2H6 become.
• 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 (see Gas Cracker 1c).
• a method 100 according to the invention in the vapor cracking method 1 can also work only with recirculated streams.
• the C3plus stream h from the deethanizer step 6 is subjected to a 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 n is subjected, for example, to a C3 separation step 12 in which essentially propylene C3H6 and propane C3H8 are formed.
• the propylene C3H6 can be a corresponding Method 100 can be taken as a product
• the propane C3H8 can in the
• Steam cracking process 1 are returned, for example, in the gas cracker 1 c.
• a C4plus fraction o, likewise formed in the depropanizer step 10, is subjected to a full or partial hydrogenation in a hydrogenation step 13, for example.
• An obtained current p is supplied to a deoctanizer step 14 in which
• the deoctanizer step 14 may, if a corresponding stream is generated, also be fed with a C5plus stream q, which is generated from the second gas mixture formed in the oxygenate-to-olefin process 2.
• the oxygenate-to-olefin process 2 is particularly useful for the reaction of
• Hydrocarbons are reacted.
• Corresponding oxygenates are supplied as stream r to one or more reactors and to an olefin-containing
• Gas mixture s implemented which is referred to here as the second gas mixture.
• the second gas mixture s which contains at least or predominantly hydrocarbons having one to five carbon atoms, is subjected to a post-treatment step 15
• Oxygenates Water obtained in a corresponding manner is drawn off as stream t, a stream u removed from oxygenates is fed to a step 16 explained below. Recovered oxygenates can be recycled as stream v to the oxygenate-to-olefin process 2.
• the current u is compressed and optionally pre-cooled. It is, as already explained above, a condensation of condensable components of the current u.
• a condensate obtained is optionally dried and subjected to a depropanizer step 17 as stream w in which a C3-minus fraction x and a C4plus-fraction y are formed from the stream w.
• the C4plus fraction y contains, for example, when using appropriate
• Catalysts in the oxygenate-to-olefin process 2 comparatively small amounts of hydrocarbons having five or more carbon atoms. at However, a separation step 18 may be required to provide appropriate
• the stream y ie a C4plus or a C4 stream, is, as also mentioned, returned to the steam cracking process 1 and split there mildly in the cracking furnace 1b.
• the C3 minus current x may be combined with a current z consisting of components that are not condensable in the condensation step 16, and a
• Oxygenate removal step 19 are subjected. One in the
• Oxygenate Removal Step 19 Separated oxygenate stream (not shown) may be combined with stream v and re-subjected to the oxygenate-to-olefin process 2. A C3 minus current freed from oxygenates, the already mentioned current e, can then be subjected to process step 4 already explained. This is optional.

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