EP3249028A1 - Procédé à émissions réduites pour la fabrication d'oléfines - Google Patents

Procédé à émissions réduites pour la fabrication d'oléfines Download PDF

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Publication number
EP3249028A1
EP3249028A1 EP16171381.3A EP16171381A EP3249028A1 EP 3249028 A1 EP3249028 A1 EP 3249028A1 EP 16171381 A EP16171381 A EP 16171381A EP 3249028 A1 EP3249028 A1 EP 3249028A1
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EP
European Patent Office
Prior art keywords
reactors
tubular reactors
tubular
heat
supplied
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Withdrawn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
EP16171381.3A
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German (de)
English (en)
Inventor
Daniel Mateos
Florian Penner
Helmut Fritz
Gunther Schmidt
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
Priority to EP16171381.3A priority Critical patent/EP3249028A1/fr
Publication of EP3249028A1 publication Critical patent/EP3249028A1/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
    • C10G9/18—Apparatus
    • C10G9/20—Tube furnaces
    • 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
    • C10G9/24—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by heating with electrical means
    • 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 low-emission process for the production of olefins and a corresponding plant according to the preambles of the respective independent claims.
  • reaction tubes In vapor cracking processes and apparatus, tube reactors are typically used whose reaction tubes are heated externally using burners.
  • the reaction tubes can be designed differently. For example, reaction tubes can first be performed in pairs in parallel and then combined to form a common reaction tube, or it can be used throughout parallel pipes. The dimensioning of the reaction tubes depends, among other things, on the inserts used.
  • one or more combustion chambers of typically up to 15 m in height and 2 to 3 m in width may be provided, in which wall and / or floor mounted burners are arranged.
  • the temperature in a combustion chamber is typically 1,000 to 1,200 ° C.
  • the one or more combustion chambers are arranged downstream of one or more so-called convection zones, in which a use of the heat of the flue gases takes place.
  • the flue gas of several combustion chambers can also be led to a common convection zone.
  • the insert, the combustion air or boiler feed water supplied to the burners may be preheated or steam generated or overheated.
  • the cracked gas formed in the radiation zone in the reaction tubes is rapidly cooled to avoid undesired further reactions (so-called quench or primary quench), for which purpose a so-called quench gas cooler is used.
  • quench gas cooler is used.
  • the cleavage gas of a plurality of reaction tubes can be combined in a common line and guided therein by a corresponding quench cooler, or the reaction tubes can run separately from each other by a quench cooler designed as a linear cooler.
  • the present invention therefore has as its object to reduce emissions, in particular of carbon dioxide, in steam cracking.
  • the present invention proposes an emission-reduced process for the production of olefins and a corresponding plant with the features of the independent patent claims.
  • Embodiments are the subject of the dependent claims and the following description.
  • Gas mixtures may include "predominantly or exclusively” one or more components as used herein, with “predominantly” for a content of at least 50%, 75%, 90%, 95%, 99%, 99.5%, 99.9 %, 99.99% or 99.999% on a molar, weight or volume basis. Gas mixtures may also be "enriched” or “depleted” in one or more components as used herein, which terms refer to a content in a source gas mixture from which the gas mixture was obtained.
  • the gas mixture is " enriched " when it is at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times or 1000 times, “depleted” if it is not more than 0.9 times, 0.5 times, 0.1 times, 0.01 times or 0.001 times the content of a component, based on the starting gas mixture.
  • hydrogen the speech, it is understood as pure hydrogen or a gas mixture containing predominantly or exclusively hydrogen.
  • Common processes for fractionation of gas mixtures from steam cracking processes include in particular the generation of fractions based on the boiling points of the components contained.
  • short names are used for corresponding fractions, indicating the carbon number of predominantly or exclusively contained hydrocarbons.
  • a "C1 fraction” is a fraction that is predominantly or exclusively methane (but conventionally possibly also hydrogen, then also called “C1 minus fraction”) contains.
  • 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 dimethylacetylene.
  • 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.
  • An essential aspect of the present invention is the use of parallel operated tube reactors in vapor cracking, some of which are powered by electrical energy, i. Electric heat, and partly heated with combustion heat. In this way, considerable emission reductions can be achieved in the context of the present invention.
  • the present invention can also provide a method in which carbon dioxide emissions no longer occur at all, so that a so-called "zero emission” method is provided.
  • tubular reactors are arranged "in parallel", this means in particular that gas mixtures provided in each case are combined with one another using these tube reactors.
  • a gas mixture provided using one of the tubular reactors would be fed to another of the tubular reactors.
  • serially arranged tubular reactors may be provided to which the combined gas mixtures of the parallel tubular reactors is supplied, or which provide a gas mixture, which is then fed to the parallel tube reactors.
  • parallel tubular reactors can also be provided to supply the parallel tubular reactors in parallel identical inserts, which can be distributed for this purpose starting in particular from a main line to the parallel tubular reactors.
  • a parallel arrangement does not exclude that a volume flow through one of the parallel tube reactors may differ significantly from a flow through another of the parallel tube reactors or that different inserts are used.
  • the present invention proposes a low-emission process for the production of olefins by steam cracking, wherein a gas mixture is provided using a plurality of tubular reactors, wherein the gas mixtures provided using the plurality of tubular reactors are combined.
  • the present invention thus uses parallel tube reactors. According to the invention, at least one, but not all, of the plurality of tubular reactors is supplied with combustion heat generated by burning at least one fuel, and at least one but not all of the plurality of tubular reactors is supplied with electrical heat generated by electrical energy ,
  • the parallel arrangement allows a special flexibility.
  • it may be provided, for example, depending on the supply of electrical energy or fuels, the respectively correspondingly heated reactors at least partially shut down and perform the process in appropriate periods in the other reactors.
  • the "multiple" tubular reactors may also comprise more than two tubular reactors. In this way, in the context of the present invention, a certain shift between the parallel tube reactors may be provided.
  • the illustrated flexible operation of the tube reactors may, for example, also provide increased quantities in times when there is an excess of electricity, for example during the day or in the case of sunshine in a photovoltaic system or in the case of high wind loads in a wind energy plant Use electrical heat.
  • fuels which can be formed as explained below using the combined gas mixtures of the plurality of tubular reactors can also be temporarily stored. This can be sensibly utilized in particular in the sense of a known "peak shaving" to a large extent incurred electrical energy.
  • the amount of electrical heat used can be reduced and instead resort to appropriate fuels for generating heat of combustion.
  • this second operating mode it is also possible to use the fuels which may be temporarily stored in the first operating mode.
  • the inventive method allows a particularly advantageous adaptation to fluctuating offers of electrical energy. Even if in periods of reduced supply of electrical energy, ie in the second method mode, if necessary, no or only a small reduction in emissions is achieved, resulting in total use of the regenerative electrical energy, however, a corresponding reduction.
  • combustion heat and electrical energy (also conventional) can be used in different proportions, depending on availability and price.
  • reaction tubes that are heated electrically can be additionally heated by combustion from the outside. It is also possible to provide side by side in a corresponding tubular reactor by means of electric heat and combustion heat heated reaction tubes, in particular in different proportions. Also purely by combustion heat and / or purely by electric heat heated tube reactors may be provided in parallel to mixed heated tubular reactors.
  • the combustion heat supplied to at least one of the plurality of tube reactors is generated by burning a methane-rich gas mixture.
  • This methane-rich gas mixture can be provided from the outside of the plant, for example in the form of natural gas, or from the plant itself. In both cases, recourse can be had to known burner concepts which are established for heating corresponding tube reactors and are therefore particularly reliable.
  • the methane-rich gas mixture may be formed using the gas mixtures provided and combined by the plurality of tubular reactors.
  • a corresponding gas mixture can be provided in a demethanizer. In this way, at least partially or at least temporarily, externally provided energy can be dispensed with.
  • fractionation of the cracking gas of a steam cracking process different fractionation processes are known from the prior art, which are also used in the context of used in the present invention and can be used for fractionation of corresponding gas mixtures.
  • Corresponding fractionation methods differ, inter alia, by the sequence of the fractionation steps. In the context of appropriate fractionation but typically the mentioned demethanizer are always used.
  • the light fraction can be separated, for example by condensation at suitable temperatures, into a fraction containing predominantly or exclusively hydrogen and into a fraction which contains predominantly or exclusively methane.
  • the separation can also be completely or partially omitted, so that a mixture of essentially hydrogen and methane is present. This is also known as the so-called Schugasfr syndrome.
  • a demethanizer ridge or front-end demethanizer fractionation can be used to fractionate the fission gas of a vapor cracking process or of a gas mixture formed from a corresponding cracking gas.
  • the demethanizer is in the first place of fractionation. Therefore, the cracked gas processed in the demethanizer or the gas mixture formed from the cracked gas contains, in addition to the hydrocarbons having two carbon atoms, hydrocarbons having three or more carbon atoms.
  • hydrocarbons having three or more in a depropanizer first or front-end depropanizer fractionation hydrocarbons having four or more carbon atoms previously separated and therefore no longer reach the demethanizer.
  • a cracking gas of a steam cracking process is suitably treated prior to fractionation. Details of this are with reference to the attached FIG. 1 illustrated.
  • This treatment comprises in particular, since the processing in a demethanizer provides a cryogenic separation, in particular the separation of carbon dioxide and the drying of the product mixture. Further, removal of, for example, carbon monoxide and other undesirable components may be made.
  • heavy hydrocarbons of the pyrolysis oil and / or pyrolysis benzine fraction are separated upstream of the demethanizer, deethanizer or depropanizer in a primary fractionation.
  • the combustion heat supplied to at least one of the several tube reactors is produced by burning a hydrogen-rich gas mixture.
  • a corresponding hydrogen-rich gas mixture can also be provided from the plant or from the plant.
  • the hydrogen-rich gas mixture can also be formed using the gas mixtures provided and combined by the several tube reactors, for example also in a demethanizer. Since in a corresponding demethanizer also a hydrogen and methane-containing fraction (the mentioned Schugasfrtress) may be incurred, these can also be used.
  • the hydrogen content in comparison to, for example, natural gas also reduces emissions here.
  • one or more combustion support gases such as air or oxygen can also be supplied to the burner (s) in one or more tube reactors heated with combustion heat.
  • one or more combustion support gases such as air or oxygen
  • the concentration of nitrogen in the combustion can be reduced. In this way, the emission of nitrogen oxides compared to known methods in which combustion air is used, can be considerably reduced.
  • a feed gas mixture to the plurality of tubular reactors, which is distributed to the tubular reactors.
  • this can also be a flexible distribution, in particular to meet the corresponding offers of electrical heat or combustion heat.
  • an extended parallel arrangement of tubular reactors can also be made.
  • two (or more) groups are provided on tube reactors arranged in parallel, with a gas mixture removed from the parallel tube reactors of one group being fed to the parallel tube reactors of another group.
  • a gas mixture removed from the parallel tube reactors of one group being fed to the parallel tube reactors of another group.
  • the plurality of tube reactors are arranged in a plurality of groups, wherein the number of tubular reactors is selected such that each of these multiple groups comprises a plurality of tubular reactors, and wherein the gas mixtures each below Use of the tube reactors of a group are provided and combined, the tube reactors are fed to another group.
  • At least one, but not all, of the plurality of tubular reactors in at least one of the plural groups, the heat of combustion and at least one but not all of the plurality of tubular reactors in the at least one of the plurality of groups may be supplied with the electric heat. It may be particularly advantageous if only at least one, but not all, of the plurality of tubular reactors in at least one of the plurality of groups only the heat of combustion and at least one but not all of the plurality of tubular reactors in the at least one of the plurality of groups supply only the electrical heat. Again, all design variants are possible, which have been explained in principle above with reference to the parallel arrangement. Reference is made to the corresponding advantages.
  • tube reactors which are arranged in series with these tube reactors arranged in parallel.
  • at least one further tubular reactor may be provided which is fed with the gas mixtures provided and combined using the several parallel tubular reactors.
  • This further tubular reactor can also be heated with electrical and / or combustion heat, as basically explained above.
  • At least one further tubular reactor by means of which use is made of a gas mixture which is fed to the several tube reactors arranged in parallel.
  • a corresponding tube reactor arranged serially in front of the parallel tube reactors can be used in particular for preheating.
  • This further Tubular reactor can also be heated with electrical and / or combustion heat, as basically explained above.
  • a method according to a particularly preferred embodiment of the present invention provides for the use of at least one compressor driven by electric energy.
  • This compressor can be used for example for so-called crude gas compression, as also explained with reference to the accompanying figures. Again, can be used to drive the compressor or regeneratively generated electrical energy.
  • the present invention also relates to a plant for the production of olefins by vapor cracking, comprising a plurality of tubular reactors adapted to each provide a gas mixture and means adapted to combine the gas mixtures provided using the plurality of tubular reactors.
  • means are provided which are adapted to supply combustion heat generated by burning at least one fuel to at least one, but not all, of the plurality of tubular reactors, and means arranged to heat at least one but not all of the plurality of tubular reactors , which is generated by means of electrical energy supply.
  • Such a system is preferably set up to carry out a method, as explained above, and has correspondingly established means for this purpose. Reference is therefore expressly made to the corresponding features and advantages of the method according to the invention, which have been expressly explained above.
  • FIG. 1 For example, an emission-reduced process for the production of olefins according to one embodiment of the present invention is illustrated schematically and designated 100 as a whole. If the method is described below, the corresponding explanations apply to a system according to an embodiment of the invention in the same way.
  • Method 100 shown includes a deethanizer-first fractionation of a cracked gas.
  • the present invention is equally suitable for use with other fractionations, for example in a deethanizer or depropanizer first fractionation.
  • one or more hydrocarbon streams a and one or more vapor streams b are fed to a plurality of tube reactors 10 arranged in parallel or whose or their reaction tubes.
  • the plurality of tube reactors 10 arranged in parallel may be preceded or followed serially by one or more tubular reactors (not shown).
  • a steam generation only in the or the tube reactors is possible.
  • the plurality of tube reactors 10 arranged in parallel in particular their convection zone or convection zones, it is possible to preheat or overheat the hydrocarbon streams and / or the steam streams or streams.
  • a steam generation is possible.
  • Other streams, such as combustion air, can be heated accordingly. Details of usable in the context of the present invention, several parallel tubular reactors 10 are in the following FIGS. 2A to 2C illustrated.
  • one or a portion of the plurality of parallel tubular reactors 10 is heated using combustion heat generated using one or more predominantly or exclusively hydrogen-containing streams c, whose or their extraction will be explained in detail below.
  • one or more further fuel streams or, for example, methane separated in the process or a heating gas stream from a demethanizer can be used alternatively or additionally to provide the heat of combustion. This is illustrated with a stream d.
  • the heating of one or more other of the plurality of parallel tube reactors 10 is carried out using electric current, as illustrated in the form of an arrow e.
  • the operation of different tubular reactors 10 using different energy sources is possible, as explained above.
  • a cracked gas is generated which can be supplied in the form of a stream f to one or more quenching devices 101.
  • a cooling device in the form of a linear cooler (primary quench) and an oil column (secondary quench, oil quench) can be used.
  • the correspondingly cooled cracked gas can be converted in the form of a stream g into a primary fractionation, where pyrolysis fuel oil can be separated in the form of a stream h.
  • the correspondingly primary-fractionated cracked gas can then be supplied in the form of a stream i to a water wash 103.
  • pyrolysis gasoline in the form of a stream k can be separated from the cracked gas by means of wash water.
  • wash water the remaining process steam is condensed.
  • the resulting water can be converted into process steam in the form of a stream I, which can be fed together with the stream b in the parallel tube reactors 10.
  • steam generation can also take place only in the tube reactors 10 or their convection zones.
  • the cracked gas Downstream of the water wash, the cracked gas may be subjected in the form of a stream m in a first compression 104, in which further pyrolysis gasoline may be obtained in the form of a stream n.
  • the current n can be combined with the current k.
  • the partially compressed cracked gas can then be an acid gas removal 105th in which, for example, carbon dioxide can be separated off in the form of a stream p.
  • the fission gas processed in this way can now be subjected to a further compression 106 in the form of a flow r.
  • the cracked gas After a corresponding compression, the cracked gas can be subjected to a drying and cooling 107 in the form of a stream s and then to a deethanization 108 in the form of a stream t.
  • a fraction can be formed which predominantly or exclusively contains hydrocarbons having three or more carbon atoms, ie a C3plus fraction. This can be subtracted in the form of a corresponding current, here illustrated with C3 +.
  • a fraction can also be formed which contains predominantly or exclusively hydrogen, methane and hydrocarbons having two carbon atoms, including ethane, ethylene and acetylene. This can be supplied to a C2 hydrogenation 109 in the form of a corresponding stream, here denoted by u.
  • acetylene can be hydrogenated to ethylene.
  • a so-called front-end hydrogenation can be used.
  • a gas mixture is obtained, which still contains predominantly or exclusively hydrogen, methane, ethane and ethylene.
  • C2minus fraction gas mixture can be supplied in the form of a stream C2- a demethanization 110.
  • demethanization 110 a predominantly or exclusively hydrogen-containing stream H 2 and a predominantly or exclusively methane-containing stream CH 4 can be formed. It is also possible first to form a stream containing hydrogen and methane, which is then separated into the predominantly or exclusively hydrogen-containing stream H 2 and the predominantly or exclusively methane-containing stream CH 4 .
  • the predominantly or exclusively hydrogen-containing stream H 2 can be used according to the embodiment of the invention shown here in the form of the current c one or a part of the plurality of parallel tubular reactors 10 for heating.
  • the predominantly or exclusively methane-containing stream CH 4 can in principle also be used for this purpose, for example as an alternative or in addition to the stream c as stream d. Hydrogen and methane-containing demethanization stream may also be used as stream d.
  • the predominantly or completely freed of hydrogen and methane fraction which now still contains predominantly or exclusively ethane and ethylene, ie a C2 fraction, can now be supplied in the form of a stream C2 to a C2 splitter 111 and in this in an ethylene and a Ethane fraction are separated.
  • the ethylene fraction can be carried out in the form of a stream of C 2 H 4 as product, the ethane fraction can be recycled in the form of a stream of C 2 H 6 in the or the tube reactors 10 and further reacted there.
  • FIG. 2 In the subfigures 2A to 2C of FIG. 2 are shown arrangements with a plurality of tubular reactors, which in a method according to an embodiment of the invention, for example, a method 100 according to FIG. 1 can be used.
  • a plurality of parallel tubular reactors are also designated here by 10, the corresponding individual reactors of the plurality of parallel tubular reactors 10 with 10a to 10d.
  • portions of a hydrocarbon stream a and a steam stream b can be supplied to the several tube reactors 10 arranged in parallel. But it is also possible in principle not to provide water and steam from a common source.
  • the tubular reactors 10a and 10b may be supplied with different hydrocarbon feeds, one of the feeds may be fed with another hydrocarbon stream, etc.
  • the distribution is arbitrary.
  • the gas mixtures provided by means of the tube reactors 10a and 10b, ie the cracked gas, are added to that already described in US Pat FIG. 1 f stream shown combined.
  • the tubular reactor 10a is heated by means of electric heat, as in FIG FIG. 1 illustrated with stream e, the tubular reactor 10b, however, heated with heat of combustion.
  • the heat of combustion is provided using the current c and / or the current d.
  • the heat of combustion can thus be provided using different fuels.
  • a plurality of tube reactors 10 arranged in parallel is followed by a further tube reactor 10c in series, which in the illustrated example is heated with combustion heat which is provided using the current c and / or the current d.
  • combustion heat which is provided using the current c and / or the current d.
  • an electric heating is possible.
  • the gas mixtures provided using the tubular reactors 10a and 10b that is, for example, a partially converted fission gas, is combined to form a stream x, which is supplied to the further tubular reactor 10c and processed there further to the stream f.
  • a plurality of tube reactors 10 arranged in parallel is preceded by a further tube reactor 10d in series, which in the example shown is heated with combustion heat which is provided using the current c and / or the current d. Alternatively or additionally, however, an electric heating is possible.
  • the gas mixtures provided using the tube reactors 10a and 10b that is, for example, a partially converted fission gas, are combined into the stream f.
  • the tubular reactor 10d, the hydrocarbon stream a can be supplied. Further, a vapor stream may be supplied to the tube reactor 10d (not illustrated).
  • the tubular reactor 10d may be used to preheat or partially react the hydrocarbons of the hydrocarbon stream a.
  • a gas mixture obtained in this case can be supplied in the form of a stream y to the plurality of tube reactors 10 arranged in parallel.
  • a plurality of tube reactors arranged in parallel can also be provided in each case.
  • a plurality of repetitive units of tube reactors 10a and 10b may be arranged in series in series in corresponding groups.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
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  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP16171381.3A 2016-05-25 2016-05-25 Procédé à émissions réduites pour la fabrication d'oléfines Withdrawn EP3249028A1 (fr)

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Cited By (11)

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EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3730592A1 (fr) * 2019-04-24 2020-10-28 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
WO2022008053A1 (fr) 2020-07-09 2022-01-13 Basf Antwerpen N.V. Procédé de vapocraquage
WO2022008052A1 (fr) 2020-07-09 2022-01-13 Basf Antwerpen N.V. Procédé de vapocraquage
WO2022069726A1 (fr) * 2020-10-02 2022-04-07 Basf Se Intégration thermique d'un réacteur chauffé électriquement
WO2022171906A2 (fr) 2021-04-28 2022-08-18 Torrgas Technology B.V. Procédé de préparation d'oléfines inférieures
EP4056892A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système de vapocraquage
EP4056893A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système pour unité de craquage à vapeur
EP4056894A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système pour unité de craquage à vapeur
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EP3725865A1 (fr) * 2019-04-17 2020-10-21 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
EP3730592A1 (fr) * 2019-04-24 2020-10-28 SABIC Global Technologies B.V. Utilisation d'énergie renouvelable dans la synthèse d'oléfine
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WO2022008052A1 (fr) 2020-07-09 2022-01-13 Basf Antwerpen N.V. Procédé de vapocraquage
WO2022069726A1 (fr) * 2020-10-02 2022-04-07 Basf Se Intégration thermique d'un réacteur chauffé électriquement
EP4056892A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système de vapocraquage
EP4056893A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système pour unité de craquage à vapeur
EP4056894A1 (fr) 2021-03-10 2022-09-14 Linde GmbH Procédé et système pour unité de craquage à vapeur
WO2022189422A1 (fr) 2021-03-10 2022-09-15 Linde Gmbh Procédé et système de vapocraquage
WO2022189424A1 (fr) 2021-03-10 2022-09-15 Linde Gmbh Procédé et système de vapocraquage
WO2022189423A1 (fr) 2021-03-10 2022-09-15 Linde Gmbh Procédé et système de vapocraquage
WO2022171906A2 (fr) 2021-04-28 2022-08-18 Torrgas Technology B.V. Procédé de préparation d'oléfines inférieures
US20230287284A1 (en) * 2021-09-01 2023-09-14 Bechtel Energy Technologies & Solutions, Inc. Systems and Methods for Producing a Decarbonized Blue Hydrogen Gas for Cracking Operations
WO2023062165A1 (fr) 2021-10-14 2023-04-20 Technip Energies France Sas Station d'éthylène comprenant un réacteur de pyrolyse à alimentation électrique et un échangeur de chaleur d'effluent d'alimentation

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