EP3839011A1 - Procédé et système de fabrication d'hydrocarbures - Google Patents

Procédé et système de fabrication d'hydrocarbures Download PDF

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Publication number
EP3839011A1
EP3839011A1 EP19218125.3A EP19218125A EP3839011A1 EP 3839011 A1 EP3839011 A1 EP 3839011A1 EP 19218125 A EP19218125 A EP 19218125A EP 3839011 A1 EP3839011 A1 EP 3839011A1
Authority
EP
European Patent Office
Prior art keywords
coke
trap
stream
heat exchanger
cracking
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Withdrawn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
EP19218125.3A
Other languages
German (de)
English (en)
Inventor
Christian Kaiser
Mario SANKTJOHANSER
Christian Ziegler
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 EP19218125.3A priority Critical patent/EP3839011A1/fr
Priority to US17/786,821 priority patent/US20230046854A1/en
Priority to PCT/EP2020/087014 priority patent/WO2021123160A1/fr
Publication of EP3839011A1 publication Critical patent/EP3839011A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • 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
    • C10G9/16—Preventing or removing incrustation
    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4037—In-situ 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • steam cracking plants (often also referred to as ethylene plants) with so-called cracking furnaces are used. These cracking furnaces can also be provided in several groups and operated under different conditions or fed with different inserts (English feeds).
  • cracked gas discharged from a cracking furnace which is initially at a temperature of typically 750 to 875 ° C, has to stop the reactions as quickly as possible and thus prevent the excessive formation of undesirable by-products should be cooled down as quickly as possible.
  • quench heat exchangers which can be subdivided in particular into so-called primary and secondary quench heat exchangers (English. Primary Quench Exchanger, Secondary Quench Exchanger), are used to cool the fission gas. Different designs are also described in the specialist literature.
  • the correspondingly cooled cracked gas is, depending on its composition, which depends in particular on the reaction inserts and cracking conditions used, a water and / or oil wash, then a compression and acid gas removal, and at least partially at cryogenic temperatures operated fractionation in order to obtain the desired products, classically ethylene, from the product stream.
  • the by-product of the steam cracking of hydrocarbons is often coke, a hard or non-volatile, carbon-containing solid that easily accumulates on the walls of the steam cracking plant.
  • the regular operation of the steam cracking plant can be interrupted, for example cyclically, as in FIG US 2005/261532 A1 described.
  • a cleaning stream containing oxygen and / or steam can be introduced into the plant in order to oxidize the coke and at least partially convert it into gaseous residues, which are discharged from the plant can.
  • a steam cracking plant according to the invention for producing a product stream containing low molecular weight hydrocarbon compounds comprises a cracking furnace, a quench heat exchanger, a coke trap and a coke collecting device.
  • the quench heat exchanger mentioned here and below is, unless stated otherwise, in particular a secondary quench heat exchanger which can be preceded by a primary quench heat exchanger.
  • primary and secondary quench heat exchangers For the function and operation of primary and secondary quench heat exchangers, reference is made to the specialist literature cited at the beginning.
  • the coke trap has an inlet which, downstream of the cracking furnace and upstream of the quench heat exchanger, is in fluid connection with a line carrying the extraction flow, or in particular the cracked gas, and an outlet which, bypassing the quench heat exchanger, is in fluid connection with the coke collecting device. Furthermore, the coke trap is set up to hold back coke particles via the inlet from the extraction flow and the coke particles via the outlet in the direction of the coke collecting device using the Withdrawal stream and eject with receipt of a stream of coke. The retention and ejection of the coke particles is carried out in particular in a periodic change.
  • the coke trap in a first operating mode, is operated in such a way that coke particles are retained in it, but the remaining components are passed into the quench heat exchanger.
  • a second operating mode which can correspond, for example, to the decoking operation mentioned, the extraction flow is passed through the coke trap into the outlet, preferably at a high flow rate, in order to convey the coke retained during the first operating mode to the coke collecting device.
  • a smaller amount of the withdrawal flow in particular none, is thus passed into the quench heat exchanger. This prevents coke formed in the cracking furnace from entering the quench heat exchanger.
  • the quench heat exchanger is set up to (possibly further) cool the withdrawal flow, in particular the cracked gas.
  • the coke trap Before or after the decoking operation (with the steam / air mixture mentioned as the extraction flow from the cracking furnace), the coke trap is emptied into the downstream system with the aid of a (partial) flow.
  • the steam cracking system comprises a further coke trap downstream of the quench heat exchanger, which has an inlet which is in fluid connection with a line carrying the extraction stream cooled in the quench heat exchanger, and an outlet which is in fluid connection with the coke collecting device.
  • connection of the outlet of the coke trap arranged upstream of the quench heat exchanger with the coke collecting device advantageously opens upstream of the coke collecting device at a shallow angle, in particular from about 45 ° or from 40 ° to 50 °, in a line opening into the coke collecting device, in particular the connection of the outlet of the further coke trap with the coke collecting device, in order to avoid damage due to abrasion or erosion on the lines that make the connection between the respective Avoid forming a trap with the coke collecting device and reducing turbulence at this point.
  • the line carrying the extraction stream advantageously has a kink or bend downstream of the cracking furnace and upstream of the quench heat exchanger, up to which the line runs in a first direction and from which the line runs in a second direction.
  • the first and the second direction advantageously enclose an angle of, for example, 30 ° to 120 °, in particular 90 °.
  • the coke trap the inlet of which is arranged downstream of the cracking furnace and upstream of the quench heat exchanger and is in fluid connection with the line carrying the extraction flow, in particular the cracked gas, is arranged such that the first direction points towards the inlet. In this way, coke particles that are entrained in the fast-flowing extraction stream can continue their trajectory due to the inertia and get into the coke trap, while a particle-free or low-particle extraction stream flows off in the second direction.
  • a line in this context, this does not necessarily mean a continuous pipe.
  • a line in the sense understood here can also be a plurality of tubes or tube sections which, possibly also connected by non-tubular intermediate areas, form a continuous fluid channel.
  • the coke collecting device advantageously comprises a cyclone, a fire box and / or a flow brake.
  • the coke can be obtained as an additional product of value if required or alternatively, preferably with the recovery of process heat, be burned if no further recycling is desired.
  • a steam generator, an insert mixer and a cracked gas cooler are preferably part of the device according to the invention.
  • the mentioned primary quench heat exchanger can also be present or used as the cracked gas cooler.
  • the cracking furnace with at least some of these components can also be combined to form a furnace module, which simplifies the construction and maintenance of such a steam cracking system and therefore enables it to be more economical.
  • a method for producing hydrocarbons using steam cracking with removal of coke from the extraction stream is also provided.
  • a feed fluid containing hydrocarbons and / or water vapor is subjected to vapor cracking while retaining a cracked gas.
  • the removal of coke from the extraction stream, which comprises the cracked gas takes place downstream of the steam cracking using a coke trap and while obtaining a coke-depleted or free extraction stream.
  • the withdrawal stream or the cracked gas is subjected to a quench heat exchange downstream of the coke trap with cooling.
  • a vapor cracking system as already described above, is preferably used for the process described.
  • quench heat exchanger can be typical transfer line heat exchangers for steam cracking systems in which several pipelines are routed through a cooling space through which water or steam flows.
  • a withdrawal stream can be provided which is essentially free of hydrocarbons, for example by suitable control of the composition of the feed fluid.
  • the gaseous constituents of the coke stream which serve as a carrier medium for the coke particles, can be released into the natural atmosphere without significant adverse effects on the environment after the coke particles have been removed therefrom in the coke collecting device.
  • a withdrawal stream containing cracked gas is used to empty the coke trap according to the invention, it must be ensured that the cracked gas from the coke stream does not get into the atmosphere, as this could cause environmental damage and is also economically nonsensical because the cracked gas is the desired product of value Steam splitting acts. It is therefore preferably separated from the coke stream in such operating modes and fed back into the process, for example into the feed fluid, the withdrawal stream or the product stream.
  • the vapor cracking system 100 comprises a cracking furnace 10, a coke trap 20, a quench heat exchanger 30 and a coke collecting device 40.
  • the hydrocarbons react at least partially with the water molecules to form a cracking gas 2, which typically also contains coke particles in addition to low molecular weight hydrocarbon compounds.
  • the cracked gas 2 is discharged from the cracking furnace 10 as extraction flow 2 and passes through the coke trap 20.
  • the pipeline that carries the extraction flow 2 can have a bend of 30 ° to 120 °, for example essentially 90 °, immediately upstream of the coke trap 20. have, so that the extraction flow 2 in the pipeline before the bend in the direction of the coke trap 20, but after the bend directly away from the coke trap 20.
  • the coke trap 20 has an inlet in the direction of the cracking furnace 10 which is open to the pipeline for fluids, that is to say is in fluid connection with the pipeline which leads the extraction flow 2 from the cracking furnace 10. Due to the higher inertia of the coke particles compared to the gaseous molecules, in particular of the low molecular weight hydrocarbon compounds, of the withdrawal stream 2, the coke particles move largely linearly into the inlet of the coke trap, while the gaseous components of the stream, in particular the low molecular weight hydrocarbon compounds, preferentially follow the curve. As a result, the extraction flow in the bend in the pipeline is depleted of coke before it is passed on in the direction of the quench heat exchanger 30. Coke is initially retained in the coke trap 20.
  • the cracked gas or the withdrawal flow is cooled in the quench heat exchanger 30, for example against the one or more feed fluids 1, and withdrawn from the system 100 via a product valve 35 as product flow 5.
  • a coke-rich stream 4 is formed from the extraction stream 2 and the coke retained in the coke trap 20, which stream is conducted to the coke collecting device 40.
  • the control valve 25 is closed again and, if necessary, the product valve 35 is opened again and / or the pressure of the extraction flow is reduced again.
  • the cracking furnace 10 is essentially operated at a pressure level that corresponds to natural atmospheric pressure, and when the pressure increases, the extraction flow 2 to a pressure level in the range between 1.2 and 2.5 times the natural atmospheric pressure is compressed.
  • the pressure in the cracking furnace 10 itself can be increased or the extraction flow 2 leaving the cracking furnace 10 can be subjected to compression downstream of the cracking furnace 10.
  • the times at which the coke trap is emptied in the manner described can be selected, for example, at regular, in particular predetermined, intervals. In certain embodiments of the invention it can also be provided that the times are selected depending on a degree of filling of the coke trap 20 or a quality parameter of the coke-depleted extraction stream 3, for example regulated or controlled.
  • sensors can be provided in or on the coke trap, for example, which monitor the degree of filling.
  • these can be light barriers that monitor a visual path through the coke trap 20 and define an upper threshold value for the degree of filling as exceeded when the visual path is blocked.
  • the system 200 shown has a further coke trap 33, which is arranged downstream of the quench heat exchanger, with a further control valve or decoking gas valve 37 assigned to it.
  • the functional principle of this further coke trap 33 is identical to that of the coke trap 20.
  • the separation of coke particles is also based here on the higher inertia of the coke particles compared to the gaseous components of the withdrawal stream 3.
  • the further coke trap 33 is emptied in an analogous manner by opening the further control valve 37 and advantageously closing the other valves 25, 35 of the system 200 and preferably with a simultaneous increase in the pressure of the extraction flow or cracked gas 2, 3.
  • the coke streams 4 of the coke trap 20 and 6 of the further coke trap 33 are combined and conducted into the coke collecting device 40.
  • an existing system can be retrofitted particularly easily with the coke trap 20 without having to significantly intervene in the piping of the other system components 30, 33, 40.
  • each coke trap 20, 33 has its own pipeline from its respective outlet to the coke collecting device 40.
  • a common coke collecting device is provided for certain coke traps 20, 33, while other coke traps 20, 33 are assigned a respective dedicated coke collecting device 40.
  • a common coke collecting device is provided for certain coke traps 20, 33, while other coke traps 20, 33 are assigned a respective dedicated coke collecting device 40.
  • the coke collecting device 40 can be designed using a cyclone, a fire box and / or a flow brake.
  • the functional principles of these components are only briefly outlined below for better understanding: the respective coke stream 4, 6 can be introduced into a cyclone, in particular tangentially.
  • the more inert coke separates from the less inert components of the coke stream in a radially outer area, in particular on a cylinder jacket wall, of the cyclone or is slowed down there by friction and sinks to a bottom of the cyclone located geodetically below.
  • the coke can be removed from the cyclone from this base.
  • Coke particles of the coke stream 4, 6 are at least partially burned and / or sintered in a fire box. This is particularly advantageous if the coke is not to be used as a by-product.
  • the heat of combustion can be taken from the fire box and used to operate the system 100, 200, for example to convert the feed fluid 1 to preheat.
  • a flow brake reduces the flow speed of the coke stream 4, 6 and thereby enables the generally denser coke particles to settle from the other constituents of the coke stream 4, 6.
  • control valve 37 or a corresponding coke flow 6 may be necessary or advantageous in order to maintain a regular decoking path, so that only the discharge system 40 can be installed separately / twice. This makes it possible to produce coke as a product (e.g. via dry coke extraction).

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP19218125.3A 2019-12-19 2019-12-19 Procédé et système de fabrication d'hydrocarbures Withdrawn EP3839011A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP19218125.3A EP3839011A1 (fr) 2019-12-19 2019-12-19 Procédé et système de fabrication d'hydrocarbures
US17/786,821 US20230046854A1 (en) 2019-12-19 2020-12-18 Method and installation for the production of hydrocarbons
PCT/EP2020/087014 WO2021123160A1 (fr) 2019-12-19 2020-12-18 Procédé et installation pour la production d'hydrocarbures

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP19218125.3A EP3839011A1 (fr) 2019-12-19 2019-12-19 Procédé et système de fabrication d'hydrocarbures

Publications (1)

Publication Number Publication Date
EP3839011A1 true EP3839011A1 (fr) 2021-06-23

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EP19218125.3A Withdrawn EP3839011A1 (fr) 2019-12-19 2019-12-19 Procédé et système de fabrication d'hydrocarbures

Country Status (3)

Country Link
US (1) US20230046854A1 (fr)
EP (1) EP3839011A1 (fr)
WO (1) WO2021123160A1 (fr)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA926622A (en) 1970-04-22 1973-05-22 Esso Research And Engineering Company Method and apparatus for minimizing coke in steam cracking
US6237341B1 (en) * 1999-03-09 2001-05-29 Kyushu Electric Power Company Boiler scale collecting device before steam turbine
US20050261532A1 (en) 2004-05-21 2005-11-24 Stell Richard C Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids
EP2096157A2 (fr) * 2008-02-22 2009-09-02 Linde AG Procédé et dispositif de commutation d'organes de verrouillage sur des fours de craquage
US20140024873A1 (en) * 2012-07-20 2014-01-23 Lummus Technology Inc. Coke catcher
EP2772524A1 (fr) * 2013-02-28 2014-09-03 Linde Aktiengesellschaft Dispositif de commutation d'un four de craquage entre un mode de production et un mode de décocage

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2728580A1 (fr) * 1994-12-26 1996-06-28 Inst Francais Du Petrole Procede et installation de vapocraquage comportant l'injection de poudres collectees en un point unique

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA926622A (en) 1970-04-22 1973-05-22 Esso Research And Engineering Company Method and apparatus for minimizing coke in steam cracking
US6237341B1 (en) * 1999-03-09 2001-05-29 Kyushu Electric Power Company Boiler scale collecting device before steam turbine
US20050261532A1 (en) 2004-05-21 2005-11-24 Stell Richard C Process and apparatus for removing coke formed during steam cracking of hydrocarbon feedstocks containing resids
EP2096157A2 (fr) * 2008-02-22 2009-09-02 Linde AG Procédé et dispositif de commutation d'organes de verrouillage sur des fours de craquage
US20140024873A1 (en) * 2012-07-20 2014-01-23 Lummus Technology Inc. Coke catcher
EP2772524A1 (fr) * 2013-02-28 2014-09-03 Linde Aktiengesellschaft Dispositif de commutation d'un four de craquage entre un mode de production et un mode de décocage

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
"Ullmann's Encyclopedia of Industrial Chemistry", 2007, article "Ethylene"

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Publication number Publication date
WO2021123160A1 (fr) 2021-06-24
US20230046854A1 (en) 2023-02-16

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