EP4551673A1 - Systèmes et procédés de production d'oléfines et/ou de composés aromatiques par un traitement aquatique à faible et moyenne gravité suivi d'un traitement aquatique à haute sévérité et d'un craquage à la vapeur - Google Patents

Systèmes et procédés de production d'oléfines et/ou de composés aromatiques par un traitement aquatique à faible et moyenne gravité suivi d'un traitement aquatique à haute sévérité et d'un craquage à la vapeur

Info

Publication number
EP4551673A1
EP4551673A1 EP23739536.3A EP23739536A EP4551673A1 EP 4551673 A1 EP4551673 A1 EP 4551673A1 EP 23739536 A EP23739536 A EP 23739536A EP 4551673 A1 EP4551673 A1 EP 4551673A1
Authority
EP
European Patent Office
Prior art keywords
unit
aquaprocessing
stream
range
produce
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Withdrawn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
EP23739536.3A
Other languages
German (de)
English (en)
Inventor
Ravichander Narayanaswamy
Prashil Prakash Lakhete
Alexander Stanislaus
Kankan Bhaumik
Mathew John
Abdulrahman Shahid SARANG
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
Publication of EP4551673A1 publication Critical patent/EP4551673A1/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Withdrawn legal-status Critical Current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
    • C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
    • C10G49/18—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 in the presence of hydrogen-generating compounds, e.g. ammonia, water, hydrogen sulfide
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/10—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only 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
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of thermal cracking in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/34—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts
    • C10G9/36—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils by direct contact with inert preheated fluids, e.g. with molten metals or salts with heated gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics

Definitions

  • the present invention generally relates to the production of olefins and/or aromatics. More specifically, the present invention relates to the production of olefins and/or aromatics from crude oil and/or heavy oil by two stages of aquaprocessing, followed by steam cracking.
  • slurry and ebullated bed hydrocrackers are used for conversion of bottom of the barrel of crude oil (z.e., crude oil fractions with highest boiling points of the crude).
  • Lighter fractions of crude oil in the vacuum gas oil range are independently sent through fixed bed hydrocrackers.
  • Investments in crude to chemicals plants are very high; and this is driven, at least in part, by the high cost of steam crackers and hydrocrackers.
  • High conversion of crude oil streams lends to coke build up in fixed bed hydrocrackers leading to less time on stream.
  • slurry and ebullated bed reactors which can handle coke, are more costly.
  • the present inventors have discovered a solution to one or more of the problems described above.
  • the solution involves producing olefins and/or aromatics by aquaprocessing of crude oil and/or heavy ends in two stages, followed by cracking.
  • fixed bed hydroprocessing units are less costly than slurry reactors and thus it is advantageous that a majority of the flow goes through the fixed bed hydroprocessing while a sub-stream only goes through the more costly slurry / ebullated bed reactor.
  • plastics, plastic pyrolysis oligomers, synthetic crude oil and/or hydrocarbon streams from plastic pyrolysis can be coprocessed, in embodiments of the invention.
  • bio oils can be co-processed with, or as an alternative to, crude oil, in embodiments of the invention.
  • Embodiments of the invention include a method of producing olefins and/or aromatics.
  • the method comprises flowing a hydrocarbon feed into a first aquaprocessing unit having a first catalyst disposed therein and aquaprocessing the hydrocarbon feed in the first aquaprocessing unit to produce a first top stream having a boiling point in a range of up to 200 °C and a first bottom stream that comprises diesel and/or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • the aquaprocessing of the hydrocarbon feed comprises contacting the hydrocarbon feed with the first catalyst at a temperature in a range of 280 to 400 °C.
  • the method further includes flowing the first bottom stream into a second aquaprocessing unit having a second catalyst disposed therein and aquaprocessing the first bottom stream in the second aquaprocessing unit to produce a second top stream having a boiling point in the range of up to 305 °C and a second bottom stream that comprises one or more of pitch, coke, and fuel oil and has a boiling point in a range of 305 to 650 °C.
  • the aquaprocessing of the first bottom stream comprises contacting the first bottom stream with the catalyst at a temperature in a range of 400 to 500 °C.
  • the method also includes processing the second top stream in a steam cracking unit to produce olefins and/or aromatics.
  • Aquaprocessing is the hydrocracking of hydrocarbons in the presence of (a) one or more catalysts and (b) a solvent to keep asphaltenes dissolved, at a temperature in the range of 280 to 550 °C and a pressure in the range of 40 to 200 barg.
  • the aquaprocessing conditions can include a hydrogen to hydrocarbon ratio from 200 to 2000 NL/L of liquid feed and the aquaprocessing can be carried out with or without added steam.
  • Embodiments of the invention include a system for producing olefins and/or aromatics.
  • the system comprises a first aquaprocessing unit having a first catalyst disposed therein and adapted to contact a hydrocarbon feed with the first catalyst at a temperature in the range of 280 to 400 °C and to produce a first top stream having a boiling point in a range of up to 200 °C and a first bottom stream that comprises diesel and/or fuel oil and that has a boiling point in a range of 305 to 650 °C.
  • the system also includes a second aquaprocessing unit that has a second catalyst disposed therein and that is in fluid communication with the first aquaprocessing unit.
  • the second aquaprocessing unit is adapted to contact the first bottom stream with the second catalyst at a temperature in a range of 400 to 500 °C and to produce a second top stream having a boiling point in a range of up to 305 °C and a second bottom stream that comprises one or more of pitch, coke, or fuel oil and that has a boiling point in a range of 305 to 650 °C.
  • the system further includes a steam cracking unit in fluid communication with the first aquaprocessing unit and the second aquaprocessing unit. And the steam cracking unit is adapted to produce olefins and/or aromatics from the first top stream and the second top stream.
  • X, Y, and/or Z can be construed as X only, Y only, Z only, or any combination of two or more items X, Y, and Z (e.g., XYZ, XY, XZ, YZ).
  • wt. % refers to a weight, volume, or molar percentage of a component, respectively, based on the total weight, the total volume, or the total moles of material that includes the component.
  • 10 moles of component in 100 moles of the material is 10 mol. % of component.
  • primarily means greater than any of 50 wt. %, 50 mol. %, and 50 vol. %.
  • “primarily” may include 50.1 wt. % to 100 wt. % and all values and ranges there between, 50.1 mol.% to 100 mol.% and all values and ranges there between, or 50.1 vol. % to 100 vol. % and all values and ranges there between.
  • FIG. 1 shows a system for producing olefins and/or aromatics, according to embodiments of the invention.
  • FIG. 1 shows system 10 for producing olefins and/or aromatics, according to embodiments of the invention.
  • FIG. 2 shows method 20 for producing olefins and/or aromatics, according to embodiments of the invention. In embodiments of the invention, method 20 is implemented using system 10.
  • FIG. 1 shows system 10 comprising separation unit 103 (e.g., a flash vessel, distillation column, and/or stripping unit), which, in embodiments of the invention is adapted to separate (a) crude oil 100 and/or (b) first heavy oil stream 101, which comprises any combination of crude oil, plastics, hydrocarbons from plastics pyrolysis, bio oil, hydrogenated bio oils, oligomers from plastics, synthetic crude oil and pyrolysis oils derived from plastic, bottom cut of crude oil cut, pyrolysis oils, and heavy residues from steam crackers (where (a) and (b) forms combined feed stream 102) to produce (1) top crude oil cut stream 104 having a boiling point in a range of up to 200 °C and (2) bottom crude oil cut stream 105, having a boiling point greater than 200 °C.
  • separation unit 103 e.g., a flash vessel, distillation column, and/or stripping unit
  • separation unit 103 can comprise one or more of the following: a flash vessel, a distillation column, and/or a stripping unit.
  • system 10 includes first aquaprocessing unit 109, which comprises first reactor unit 110 and first separation unit 112.
  • first aquaprocessing unit 109 is adapted to receive hydrogen stream 107 and hydrocarbon feed 108, which comprises, in embodiments of the invention, bottom crude oil cut stream 105 and second heavy oil stream 106, recycle pyrolysis oil from steam cracker and optionally water.
  • first reactor unit 110 is adapted to receive hydrocarbon feed 108 and hydrogen stream 107.
  • First reactor unit 110 in embodiments of the invention, comprises a fixed bed reactor, has a first catalyst disposed therein, and is adapted to contact hydrogen stream 107 and hydrocarbon feed 108 with the first catalyst at a temperature in a range of 280 to 400 °C to produce first reactor unit effluent 111.
  • first separation unit 112 comprises one or more distillation columns and is adapted to receive and separate first reactor unit effluent 111 to produce first top stream 113, intermediate stream 114, and first bottom stream 115.
  • first top stream 113 has a boiling point in a range of up to 200 °C
  • intermediate stream 114 has a boiling point in a range of 200 to 305 °C
  • first bottom stream 115 comprises diesel and/or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • system 10 further comprises second aquaprocessing unit 116, which comprises second reactor unit 117 and second separation unit 119.
  • second reactor unit 117 is in fluid communication with first aquaprocessing unit 109 and is adapted to receive first bottom stream 115.
  • Second reactor unit 117 in embodiments of the invention, comprises an ebullated reactor and/or a slurry reactor, has a second catalyst disposed therein, and is adapted to contact first bottom stream 115 with the second catalyst at a temperature in the range of 400 to 500 °C to produce second reactor unit effluent 118.
  • second separation unit 119 comprises one or more distillation columns and is adapted to receive and separate second reactor unit effluent 118 to produce second top stream 120 and second bottom stream 121.
  • second top stream 120 has a boiling point in a range of up to 305 °C and second bottom stream 121 comprises one or more of pitch, coke, or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • System 10 in embodiments of the invention, includes steam cracking unit 122 is in fluid communication with separation unit 103, first aquaprocessing unit 109, and second aquaprocessing unit 116 such that top crude oil cut stream 104, first top stream 113, intermediate stream 114, and/or second top stream 120 can be flowed to steam cracking unit 122 for processing to produce high value chemicals stream 123 that comprises olefins and/or aromatics.
  • FIG. 2 shows method 20, in embodiments of the invention, includes block 200, which involves flowing (a) crude oil 100 and/or (b) first heavy oil stream 101, comprising any combination of crude oil, plastics, hydrocarbons from plastics pyrolysis, bio oil, hydrogenated bio oils, oligomers from plastics, synthetic crude oil and pyrolysis oils derived from plastic, bottom cut of crude oil cut, pyrolysis oils, and heavy residues from steam crackers (where (a) and (b) forms combined feed stream 102) to separation unit 103.
  • first heavy oil stream 101 comprising any combination of crude oil, plastics, hydrocarbons from plastics pyrolysis, bio oil, hydrogenated bio oils, oligomers from plastics, synthetic crude oil and pyrolysis oils derived from plastic, bottom cut of crude oil cut, pyrolysis oils, and heavy residues from steam crackers (where (a) and (b) forms combined feed stream 102) to separation unit 103.
  • separation unit 103 separates (a) crude oil 100 and/or (b) first heavy oil stream 101 to produce (1) top crude oil cut stream 104 having a boiling point in a range of up to 200 °C and (2) bottom crude oil cut stream 105, having a boiling point greater than 200 °C.
  • method 20 includes flowing bottom crude oil cut stream 105 and/or second heavy oil stream 106 to first aquaprocessing unit 109.
  • bottom crude oil cut stream 105 and/or second heavy oil stream 106 is combined to form hydrocarbon feed 108.
  • first reactor unit 110 which comprises a fixed bed reactor and has a first catalyst (e.g., fixed bed hydrocracking commercial catalysts with high activity: a catalyst that comprises one or more of the following: an organometallic compound having one or more of Ni, Mo, Co,W, Zr; NiMo; NiCoMo; NiMoW; alumina; and zeolite) disposed therein, is used to contact hydrocarbon feed 108 and hydrogen stream 107, optionally water and recycle pyrolysis oil from steam cracker with the first catalyst at a temperature in a range of 280 to 400 °C to produce first reactor unit effluent 111.
  • a first catalyst e.g., fixed bed hydrocracking commercial catalysts with high activity: a catalyst that comprises one or more of the following: an organometallic compound having one or more of Ni, Mo, Co,W, Zr; NiMo; NiCoMo; NiMoW; alumina; and zeolite
  • first reactor unit effluent 111 is flowed to first separation unit 112.
  • first separation unit 112 which can comprise one or more distillation columns, receives and separates first reactor unit effluent 111 to produce first top stream 113, intermediate stream 114, and first bottom stream 115.
  • first top stream 113 has a boiling point in a range of up to 200 °C
  • intermediate stream 114 has a boiling point in a range of 200 to 305 °C
  • first bottom stream 115 comprises diesel and/or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • method 20 further comprises, at block 207, flowing first bottom stream 115 into second aquaprocessing unit 116, which comprises second reactor unit 117 and second separation unit 119.
  • second reactor unit 117 which comprises an ebullated reactor and/or a slurry reactor and has a second catalyst (e.g., fixed bed hydrocracking commercial catalysts with high activity: a catalyst that comprises one or more of the following: an organometallic compound having one or more of Ni, Mo, Co,W, Zr; NiMo; NiCoMo; NiMoW; alumina; and zeolite) disposed therein, is used to contact first bottom stream 115 with hydrogen, optional water and recycle pyrolysis oil from steam crackers with the second catalyst at a temperature in the range of 400 to 500 °C to produce second reactor unit effluent 118.
  • a catalyst e.g., fixed bed hydrocracking commercial catalysts with high activity: a catalyst that comprises one or more of the following: an organometallic compound having one or more of Ni, Mo
  • second reactor unit effluent 118 is flowed to second separation unit 119.
  • second separation unit 119 which can comprise one or more distillation columns, receives and separates second reactor unit effluent 118 to produce second top stream 120 and second bottom stream 121.
  • second top stream 120 has a boiling point in the range of up to 305 °C and second bottom stream 121 comprises one or more of pitch, coke, or fuel oil and has a boiling point in a range of 305 to 650
  • Method 20 in embodiments of the invention, includes, at block 211, flowing top crude oil cut stream 104, first top stream 113, intermediate stream 114, and/or second top stream 120 to steam cracking unit 122. And at block 212, embodiments of the invention involve steam cracking unit 122 processing top crude oil cut stream 104, first top stream 113, intermediate stream 114, and/or second top stream 120 to produce high value chemicals stream 123, which comprises olefins and/or aromatics.
  • the olefins produced at block 212 includes ethylene, propylene, butenes, butadienes, and the aromatics include benzene, toluene, xylene, and ethyl benzene.
  • the systems and processes described herein can also include various equipment that is not shown and is known to one of skill in the art of chemical processing. For example, some controllers, piping, computers, valves, pumps, heaters, thermocouples, pressure indicators, mixers, heat exchangers, and the like may not be shown.
  • Embodiment 1 is a method of producing olefins and/or aromatics.
  • the method includes flowing a hydrocarbon feed and hydrogen, along with optional water and recycle pyrolysis oil from steam cracker into a first aquaprocessing unit having a first catalyst disposed therein.
  • the method further includes aquaprocessing the hydrocarbon feed in the first aquaprocessing unit to produce a first top stream having a boiling point in a range of up to 200 °C and a first bottom stream that includes diesel and/or fuel oil and has a boiling point in a range of 305 to 650 °C, wherein the aquaprocessing of the hydrocarbon feed includes contacting the hydrocarbon feed and the hydrogen with the first catalyst at a temperature in a range of 280 to 400 °C.
  • the method still further includes flowing the first bottom stream into a second aquaprocessing unit having a second catalyst disposed therein.
  • the method includes aquaprocessing the first bottom stream along with hydrogen, optional water and recycle pyrolysis oil in the second aquaprocessing unit to produce a second top stream having a boiling point in a range of up to 305 °C and a second bottom stream that comprises one or more of pitch, coke, or fuel oil and has a boiling point in a range of 305 to 650 °C, wherein the aquaprocessing of the first bottom stream includes contacting the first bottom steam with the second catalyst at a temperature in a range of 400 to 500 °C.
  • the method also includes processing the second top stream in a steam cracking unit to produce olefins and/or aromatics.
  • Embodiment 2 is the method of embodiment 1, wherein, within the first aquaprocessing unit, the contacting of the hydrocarbon feed and hydrogen with the first catalyst is carried out in a first reactor unit to produce a first reactor unit effluent, and the method further includes separating the first reactor unit effluent in a first separation unit within the first aquaprocessing unit.
  • Embodiment 3 is the method of embodiment 1, wherein, within the second aquaprocessing unit, the contacting of the first bottom stream with the second catalyst is carried out in a second reactor unit to produce a second reactor unit effluent, and the method further includes separating the second reactor unit effluent in a second separation unit within the second aquaprocessing unit.
  • Embodiment 4 is the method of embodiment 1, wherein the olefins comprise ethylene and/or propylene and the aromatics comprise benzene.
  • Embodiment 5 is the method of embodiment 1, wherein the first aquaprocessing unit includes a fixed bed reactor.
  • Embodiment 6 is the method of embodiment 1, wherein the second aquaprocessing unit includes an ebullated reactor and/or a slurry reactor.
  • Embodiment 7 is the method of embodiment 1, wherein the hydrocarbon feed comprises one or more of the following: crude oil, plastics, oligomers from plastic pyrolysis, synthetic crude oil, bottom crude oil cut, bio oil, and hydrocarbons from plastics pyrolysis.
  • Embodiment 8 is the method of embodiment 7, wherein the hydrocarbon feed comprises a bottom crude oil cut stream and the method further includes distilling crude oil in a separation unit to produce the bottom crude oil cut stream and a top crude oil cut stream having a boiling point in a range of up to 200 °C.
  • Embodiment 9 is the method of embodiment 8, further including processing the top crude oil cut stream in the steam cracking unit to produce olefins.
  • Embodiment 10 is the method of embodiment 1, further including processing the first top stream in the steam cracking unit to produce olefins.
  • Embodiment 11 is the method of embodiment 1, further including withdrawing an intermediate stream from the first aquaprocessing unit, the intermediate stream having a boiling point in a range of 200 to 305 °C, and processing the intermediate stream in the steam cracking unit to produce olefins.
  • Embodiment 12 is the method of embodiment 1, wherein the first catalyst comprises one or more of: an organometallic compound having one or more of Ni, Mo, Co, W, Zr; NiMo; NiCoMo; NiMoW; alumina and/or zeolite.
  • Embodiment 13 is the method of embodiment 1, wherein the second catalyst comprises particulate hydrocracking catalyst with or without dissolved catalyst.
  • Embodiment 14 is a system for producing olefins and/or aromatics.
  • the system includes a first aquaprocessing unit having a first catalyst disposed therein and adapted to contact a hydrocarbon feed and hydrogen with the first catalyst at a temperature in a range of 280 to 400 °C and to produce a first top stream having a boiling point in a range of up to 305 °C or less and a first bottom stream that comprises diesel and/or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • the system further includes a second aquaprocessing unit having a second catalyst disposed therein and in fluid communication with the first aquaprocessing unit, the second aquaprocessing unit adapted to contact the first bottom stream with the second catalyst at a temperature in a range of 400 to 500 °C and to produce a second top stream having a boiling point in a range of up to 305 °C and a second bottom stream that comprises one or more of pitch, coke, or fuel oil and has a boiling point in a range of 305 to 650 °C.
  • the method still further includes a steam cracking unit in fluid communication with the first aquaprocessing unit and the second aquaprocessing unit, the steam cracking unit adapted to produce olefins and/or aromatics from the first top stream and the second top stream.
  • Embodiment 15 is the system of embodiment 14, wherein the first aquaprocessing unit includes a fixed bed reactor.
  • Embodiment 16 is the system of embodiment 14, wherein the second aquaprocessing unit includes an ebullated reactor and/or a slurry reactor.
  • Embodiment 17 to 20 is the system of embodiment 14 further including a separation unit (a flash vessel, a distillation column, and/or a stripping unit) adapted to separate crude oil to produce a bottom crude oil cut stream that is included in the hydrocarbon feed to the first aquaprocessing unit.
  • a separation unit a flash vessel, a distillation column, and/or a stripping unit
  • Embodiment 18 is the system of embodiment 14, wherein the separation unit is a flash vessel in fluid communication with the steam cracking unit and the system is adapted to flow a top crude oil cut stream having a boiling point in a range of up to 200 °C from the separation unitto the steam cracking unit.
  • Embodiment 19 is The system of claim 17, wherein the separation unit is a distillation column in fluid communication with the steam cracking unit and the system is adapted to flow a top crude oil cut stream having a boiling point in a range of up to 220 °C from the distillation column to the steam cracking unit.
  • Embodiment 20 is the system of claim 17, wherein the separation unit is a stripping unit where the top crude oil cut is separated by use of a stripping gas with the stripping gas being hydrogen, saturated gases Cl to C4.
  • the stripping unit is in fluid communication with the steam cracking unit and the system is adapted to flow a top crude oil cut stream having a boiling point in a range of up to 220 °C from the stripping unit to the steam cracking unit.
  • Embodiment 21 is the system of embodiment 14, wherein the first aquaprocessing unit includes one or more distillation columns.
  • Embodiment 22 is the system of embodiment 14, wherein the second aquaprocessing unit includes one or more distillation columns.
  • Embodiment 23 is the system of embodiment 14, wherein pyrolysis oil recycled from steam cracker is preferentially routed to second aquaprocessing unit as compared to first aquaprocessing unit. This is because the second aquaprocessng unit operates at higher severity and conversion over the first unit and as a result, it is required to reduce asphaltene / coke aggregation.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne des systèmes et des procédés de production d'oléfines et ou des composés aromatiques. Les procédés comprennent l'utilisation de deux étapes de traitement à l'eau d'huiles brutes et/ou lourdes avant un traitement ultérieur dans une unité de vapocraquage pour produire des oléfines et/ou des composés aromatiques. La première étape de traitement à l'eau et la seconde étape de traitement à l'eau fonctionnent à différentes sévérités. Les systèmes comprennent deux unités de traitement à l'eau pouvant fonctionner à différentes sévérités.
EP23739536.3A 2022-07-09 2023-07-06 Systèmes et procédés de production d'oléfines et/ou de composés aromatiques par un traitement aquatique à faible et moyenne gravité suivi d'un traitement aquatique à haute sévérité et d'un craquage à la vapeur Withdrawn EP4551673A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
IN202241039482 2022-07-09
PCT/EP2023/068768 WO2024012995A1 (fr) 2022-07-09 2023-07-06 Systèmes et procédés de production d'oléfines et/ou de composés aromatiques par un traitement aquatique à faible et moyenne gravité suivi d'un traitement aquatique à haute sévérité et d'un craquage à la vapeur

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EP4551673A1 true EP4551673A1 (fr) 2025-05-14

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EP23739536.3A Withdrawn EP4551673A1 (fr) 2022-07-09 2023-07-06 Systèmes et procédés de production d'oléfines et/ou de composés aromatiques par un traitement aquatique à faible et moyenne gravité suivi d'un traitement aquatique à haute sévérité et d'un craquage à la vapeur

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US (1) US20250326973A1 (fr)
EP (1) EP4551673A1 (fr)
KR (1) KR20250033220A (fr)
CN (1) CN119522271A (fr)
WO (1) WO2024012995A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5885441A (en) * 1997-04-11 1999-03-23 Intevep, S.A. Steam conversion process and catalyst
WO2020157595A1 (fr) * 2019-01-29 2020-08-06 Sabic Global Technologies B.V. Procédés et systèmes de valorisation d'huiles brutes, d'huiles lourdes et de résidus

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CN119522271A (zh) 2025-02-25
WO2024012995A1 (fr) 2024-01-18
US20250326973A1 (en) 2025-10-23
KR20250033220A (ko) 2025-03-07

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