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WO2024013002A1 - Systèmes et procédés de production de produits oléfiniques à partir de charges d'hydrocarbures - Google Patents

Systèmes et procédés de production de produits oléfiniques à partir de charges d'hydrocarbures Download PDF

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Publication number
WO2024013002A1
WO2024013002A1 PCT/EP2023/068779 EP2023068779W WO2024013002A1 WO 2024013002 A1 WO2024013002 A1 WO 2024013002A1 EP 2023068779 W EP2023068779 W EP 2023068779W WO 2024013002 A1 WO2024013002 A1 WO 2024013002A1
Authority
WO
WIPO (PCT)
Prior art keywords
ethane
cracking unit
steam cracking
stream
mixed feed
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.)
Ceased
Application number
PCT/EP2023/068779
Other languages
English (en)
Inventor
Kenneth Francis LAWSON
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.)
SABIC Global Technologies BV
Original Assignee
SABIC Global Technologies BV
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 SABIC Global Technologies BV filed Critical SABIC Global Technologies BV
Priority to CN202380052742.6A priority Critical patent/CN119522269A/zh
Priority to EP23741617.7A priority patent/EP4551670A1/fr
Priority to KR1020257000470A priority patent/KR20250033215A/ko
Publication of WO2024013002A1 publication Critical patent/WO2024013002A1/fr
Anticipated expiration legal-status Critical
Ceased 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/023—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only only thermal cracking steps
    • 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 generally concerns systems and methods for producing olefin products from a hydrocarbon feedstock.
  • a system can include a mixed feed steam cracking unit coupled to an ethane steam cracking unit where the mixed feed steam cracking unit produces olefins and ethane.
  • the ethane can be further processed in the ethane steam cracking unit to produce ethylene and C2+ hydrocarbons.
  • the C2+ hydrocarbons can be recycled to the mixed feed steam cracking unit.
  • Olefins e.g., ethylene
  • Naturally occurring sources of olefins do not exist in commercial quantities. Therefore, polymer producers rely on methods for converting the more abundant lower alkanes into olefins.
  • the method of choice for today's commercial scale producers is steam cracking, a highly endothermic process where steam-diluted alkanes are subjected briefly to a temperature of at least 800 °C.
  • the fuel demand to produce the required temperatures and the need for equipment that can withstand that temperature add significantly to the overall cost.
  • the high temperature promotes the formation of coke which accumulates within the system, resulting in the need for costly periodic reactor shut-down for maintenance and coke removal.
  • MFC Mixed Feed Cracker
  • a MFC can handle from light hydrocarbons such as ethane, propane, and butane through naphtha up to heavy liquid feedstocks such as gas oils and hydrocracker residues to produce gasoline and a majority of petrochemical industry products.
  • a MFC process can be operated depending on the optimized downstream value chain between the oil or gas availability as feedstock and the market prices in high added value hydrocarbon products.
  • mixed feed steam cracker suffer in that they do no convert all material to olefins.
  • Optimal performance of cracking units occurs when fed with compatible feeds.
  • a dedicated furnace is usually required for optimal ethane cracking. This results in different types and sizes of furnaces.
  • Steam cracking can result in the slow deposition of coke, a form of carbon, on the reactor walls. Decoking requires the furnace to be isolated from the process and then a flow of steam or a steam/air mixture is passed through the furnace coils. This converts the hard solid carbon layer to carbon monoxide and carbon dioxide. Once this reaction is complete, the furnace is returned to service.
  • the MRC Due to the amount of coking that occurs in the MRC when ethane is cracked, the MRC generally requires at least two compatible furnaces for the cracking of ethane, which can compromise the size of the furnaces in the MRC and make the process less efficient and more cost intensive.
  • the discovery can include a system that provides an ethane cracking unit downstream of a mixed feed cracking unit. Ethane is diverted from the mixed feed cracking unit and provided to the ethane cracking unit. This set-up can reduce costs associated with upgrading the cracker feeds due to reducing the amount of energy needed to process ethane in the mixed feed steam cracking unit. Also, this setup up allows an increase in the amount of liquid hydrocarbons that can be fed to the mixed feed steam cracking unit.
  • One system can include a mixed feed steam cracking unit capable of producing an olefin product stream and an ethane (C2) product stream, an ethane steam cracking unit capable of producing a C2+ stream, and a first conduit coupled to the mixed feed steam cracking unit and the ethane steam cracking unit, and a second conduit coupled to the ethane steam cracking unit and the mixed feed stream cracking unit.
  • the first conduit can be capable of receiving the C2 product stream from the mixed feed steam cracking unit and providing the C2 product stream to the ethane steam cracking unit.
  • the second conduit can be capable of receiving the C2+ stream from the ethane steam cracking unit and providing at least a portion of (e.g., 5, 10, 15, 20, 25, 30, 35, 40, 45, 50, 55, 60, 65, 70, 75, 80, 85, 90, or 95 wt. % or more or any range therein) or all of the C2+ stream to the mixed feed stream cracking unit.
  • the first and second conduits can each directly couple the mixed feed steam cracking unit to the ethane steam cracker.
  • the system can also include a feed conduit coupled to the mixed feed steam cracking unit.
  • the system can include an ethane feed conduit coupled to the ethane steam cracking unit.
  • the ethane feed conduit can be configured to provide additional ethane to the ethane steam cracking unit.
  • the ethane cracking unit is not comprised in the mixed feed steam cracking unit.
  • the C2+ stream can include propane, propylene, butane, butylene, pentane, pentylene, and/or C6+ products.
  • the C2+ stream can also include ethane and/or ethylene.
  • a process can include step (a) where in a mixed feed steam cracking unit, a mixed hydrocarbon feed stream is subjected to conditions sufficient to produce olefin products and ethane (C2) hydrocarbons.
  • a mixed hydrocarbon feed stream can include naphtha, gas oil, middle distillate, or a combination thereof.
  • the conditions in step (a) can include a temperature and pressure such that a majority of ethane present is not cracked.
  • the conditions in step (a) can include a temperature of 600 °C to 770 °C and/or a pressure of 0.2 MPa to 0.3 MPa
  • the C2 hydrocarbons can be separated from the olefin products to produce a C2 hydrocarbon stream and an olefin products stream.
  • the C2 hydrocarbon stream can be subjected to an ethane steam cracking unit under conditions sufficient to produce a C2+ hydrocarbons stream.
  • Ethylene can be produced in addition to the C2+ hydrocarbons stream.
  • the ethylene can be stored, transported or provided to other processing units.
  • step (c) can include a temperature of 775 °C to 860 °C and/or a pressure of 0.2 MPa to 0.3 MPa
  • step (d) the C2+ hydrocarbons stream can be subjected to the mixed feed steam cracking unit.
  • a second ethane feed stream can be provided to the ethane steam cracking unit.
  • C# hydrocarbons wherein “#” is a positive integer, is meant to describe all hydrocarbons having # carbon atoms.
  • C#+ hydrocarbons is meant to describe all hydrocarbon molecules having # or more carbon atoms.
  • C2+ hydrocarbons is meant to describe a mixture of hydrocarbons having 2 or more carbon atoms.
  • C2+ alkanes accordingly relates to alkanes having 2 or more carbon atoms.
  • Cracking refers to a process involving decomposition and molecular recombination of organic compounds to produce a greater number of molecules than were initially present. In cracking, a series of reactions take place accompanied by a transfer of hydrogen atoms between molecules. For example, naphtha may undergo a thermal cracking reaction to form ethene and hydrogen.
  • Hydrocarbons are generally defined as molecules formed primarily by carbon and hydrogen atoms. Hydrocarbons may also include other elements such as, but not limited to, halogens, metallic elements, nitrogen, oxygen, and/or sulfur. Hydrocarbon fluids may include, entrain, or be entrained in non-hydrocarbon fluids such as hydrogen, nitrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water, and/or ammonia.
  • the terms “about” or “approximately” are defined as being close to as understood by one of ordinary skill in the art. In one non-limiting embodiment, the terms are defined to be within 10%, preferably within 5%, more preferably within 1%, and most preferably within 0.5%.
  • the terms “wt.%”, “vol.%”, or “mol.%” refers to a weight percentage of a component, a volume percentage of a component, or molar percentage of a component, respectively, based on the total weight, the total volume of material, or total moles, that includes the component. In a non-limiting example, 10 grams of component in 100 grams of the material is 10 wt.% of component.
  • the systems and processes of the present invention can “comprise,” “consist essentially of,” or “consist of’ particular ingredients, components, compositions, etc. disclosed throughout the specification.
  • a basic and novel characteristic of the systems and methods of the present invention are their abilities to produce olefin products (e.g., ethylene) in a cost and energy efficient manner by having an ethane steam cracker unit capable of receiving ethane from a mixed feed steam cracker unit and feeding the C2+ products produced by the ethane steam cracker unit to the mixed feed steam cracker unit.
  • FIG. 1 illustrates an embodiment of a system to produce olefin products from a hydrocarbon feed provided to a mixed hydrocarbon feed steam cracking unit.
  • the mixed hydrocarbon feed can be fed to a mixed hydrocarbon steam cracking unit to produce petroleum products and ethane.
  • the ethane can be provided to an independent ethane cracking unit to produce ethylene and/or a C2+ hydrocarbons stream, which can be recycled to the mixed hydrocarbon steam cracking unit.
  • An advantage of this set-up is that the mixed hydrocarbon steam cracking unit can be operated at optimal conditions for C2+ cracking while the ethane steam cracking unit can be operated at optimal conditions to crack ethane.
  • System 100 for producing olefin products is described.
  • System 100 can include a feed preparation unit 102, a mixed feed steam cracking unit 104, and an ethane steam cracking unit 106.
  • Crude oil 108 enters feed separation 102.
  • Crude oil can be the petroleum extracted from geologic formations in its unrefined form.
  • the term crude oil can also include petroleum that has been subjected to water-oil separations and/or gas-oil separation and/or desalting and/or stabilization.
  • Non-limiting examples of crude oil include Arabian Heavy, Arabian Light, other Gulf crudes, Brent, North Sea crudes, North and West African crudes, Indonesian, Chinese crudes, West Texas crude, and mixtures thereof, but also shale oil, tar sands, gas condensates and bio-based oils.
  • the crude oil used as feed to the process of the present invention preferably is conventional petroleum having an API gravity of more than 20° API as measured by the ASTM D287 standard.
  • the crude oil used in the process of the present invention is a light crude oil having an API gravity of more than 30° API.
  • the crude oil used in the process of the present invention can include Arabian Light Crude Oil.
  • Arabian Light Crude Oil typically has an API gravity of between 32-36° API and a sulfur content of between 1.5- 4.5 wt. %.
  • the crude oil can be separated into different crude oil fractions based on a difference in boiling point.
  • the crude oil can be distilled using a fractionating column, or a combination of more than one fractionation column, that is used to separate crude oil into fractions by fractional distillation.
  • the resulting crude oil can be processed in an atmospheric distillation unit to separate gas oil and lighter fractions from higher boiling components to produce a mixed hydrocarbon feed 110.
  • Mixed hydrocarbon feed can include hydrocarbons having a boiling point above 560 °C.
  • Non-limiting examples of various distillate hydrocarbon feeds having a boiling point above 560 °C include vacuum gas oil, middle distillate, naphtha, kerosene, liquid petroleum gas, or a blend thereof.
  • Mixed hydrocarbon feed 110 can exit feed treatment unit 102 and enter mixed feed cracking unit 104.
  • the mixed feed is subjected to steam cracking at a temperature of 600 °C to 770 °C (e.g., 600 °C, 625 °C, 650 °C, 675 °C, 700 °C, 725 °C, 950 °C, 770 °C, or any value or range there between) and/or a pressure of 0.2 MPa to 0.3 MPa (e.g., 0.2 MPa, 0.21 MPa, 0.22 MPa, 0.23 MPa, 0.24 MPa, 0.25 MPa, 0.26 MPa, 0.27 MPa, 0.28 MPa, 0.30 MPa, or any value or range there between).
  • the ethane may not be cracked.
  • the saturated hydrocarbons are broken down into smaller, often unsaturated, hydrocarbons such as ethylene and propylene by diluting the mixed hydrocarbon feed with steam and heating the mixture in a furnace in the absence presence of oxygen.
  • the steam cracking reaction can have a residence times of 50-1000 milliseconds.
  • Mixed steam cracking unit can have a fractionation unit (not shown) or a gas fractionation unit (not shown) capable of separating ethane from the olefin product stream. Such fractionation units are well known in the art.
  • Ethane stream 112 can exit mixed hydrocarbon feed steam cracking unit 104, and enter ethane steam cracking unit 106.
  • Olefin product stream 114 can exit mixed feed steam cracking unit 104 and be stored, transported or used in other processing units.
  • additional ethane stream 116 can enter ethane steam cracking unit 106.
  • the ethane stream can include other gaseous compounds such as propane and butane.
  • gaseous ethane can be diluted with steam and heated to a temperature of 775 °C to 860 °C (e.g., 775 °C, 800 °C, 825 °C, 850 °C, 860 °C, or any value or range there between) and/or a pressure of 0.2 MPa to 0.3 MPa (e.g., 0.2 MPa, 0.21 MPa, 0.22 MPa, 0.23 MPa, 0.24 MPa, 0.25 MPa, 0.26 MPa, 0.27 MPa, 0.28 MPa, 0.30 MPa, or any value or range there between) in one or more furnaces to produce ethylene and/or C2+ hydrocarbons.
  • C2+ hydrocarbons stream 118 can exit ethane steam cracking unit 106 and enter mixed feed steam cracker 104 to be further processed. In some embodiments, C2+ hydrocarbon stream 118 is not recycled to mixed feed steam cracking unit 104.

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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)

Abstract

L'invention concerne un système et un procédé de production de produits oléfiniques à partir d'une charge d'hydrocarbures. Le système peut comprendre une unité de craquage de vapeur d'alimentation mixte couplée à une unité de craquage de vapeur d'éthane, l'unité de craquage de vapeur d'alimentation mixte produisant des oléfines et de l'éthane. L'éthane peut en outre être traité dans l'unité de vapocraquage d'éthane pour produire de l'éthylène et des hydrocarbures C2+. Les hydrocarbures C2+ peuvent être recyclés vers l'unité de vapocraquage d'alimentation mixte.
PCT/EP2023/068779 2022-07-09 2023-07-06 Systèmes et procédés de production de produits oléfiniques à partir de charges d'hydrocarbures Ceased WO2024013002A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
CN202380052742.6A CN119522269A (zh) 2022-07-09 2023-07-06 由烃类原料生产烯烃产品的系统和方法
EP23741617.7A EP4551670A1 (fr) 2022-07-09 2023-07-06 Systèmes et procédés de production de produits oléfiniques à partir de charges d'hydrocarbures
KR1020257000470A KR20250033215A (ko) 2022-07-09 2023-07-06 탄화수소 공급원료로부터 올레핀 생성물을 생산하기 위한 시스템 및 공정

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN202241039488 2022-07-09
IN202241039488 2022-07-09

Publications (1)

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WO2024013002A1 true WO2024013002A1 (fr) 2024-01-18

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PCT/EP2023/068779 Ceased WO2024013002A1 (fr) 2022-07-09 2023-07-06 Systèmes et procédés de production de produits oléfiniques à partir de charges d'hydrocarbures

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EP (1) EP4551670A1 (fr)
KR (1) KR20250033215A (fr)
CN (1) CN119522269A (fr)
WO (1) WO2024013002A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1860087A1 (fr) * 2006-05-22 2007-11-28 Total Petrochemicals Research Feluy Préparation de propylène et d'ethylène à partir de butane et éthane
US20170088482A1 (en) * 2014-02-07 2017-03-30 Linde Aktiengesellschaft Process and plant for producing olefins
US9670418B2 (en) * 2012-08-09 2017-06-06 Linde Aktiengesellschaft Process for preparing olefins by thermal steamcracking
WO2017133975A1 (fr) 2016-02-05 2017-08-10 Sabic Global Technologies B.V. Procédé et installation de conversion de pétrole brut en composés pétrochimiques à rendement amélioré en produit
US20190177626A1 (en) * 2016-10-11 2019-06-13 Sabic Global Technologies B.V. Maximizing high-value chemicals from mixed plastic using different steam-cracker configurations

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1860087A1 (fr) * 2006-05-22 2007-11-28 Total Petrochemicals Research Feluy Préparation de propylène et d'ethylène à partir de butane et éthane
US9670418B2 (en) * 2012-08-09 2017-06-06 Linde Aktiengesellschaft Process for preparing olefins by thermal steamcracking
US20170088482A1 (en) * 2014-02-07 2017-03-30 Linde Aktiengesellschaft Process and plant for producing olefins
WO2017133975A1 (fr) 2016-02-05 2017-08-10 Sabic Global Technologies B.V. Procédé et installation de conversion de pétrole brut en composés pétrochimiques à rendement amélioré en produit
US20190177626A1 (en) * 2016-10-11 2019-06-13 Sabic Global Technologies B.V. Maximizing high-value chemicals from mixed plastic using different steam-cracker configurations

Also Published As

Publication number Publication date
KR20250033215A (ko) 2025-03-07
CN119522269A (zh) 2025-02-25
EP4551670A1 (fr) 2025-05-14

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