WO2024075042A1 - Procédés et systèmes d'intégration d'opérations pétrochimiques et de raffinage - Google Patents

Procédés et systèmes d'intégration d'opérations pétrochimiques et de raffinage Download PDF

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Publication number
WO2024075042A1
WO2024075042A1 PCT/IB2023/059972 IB2023059972W WO2024075042A1 WO 2024075042 A1 WO2024075042 A1 WO 2024075042A1 IB 2023059972 W IB2023059972 W IB 2023059972W WO 2024075042 A1 WO2024075042 A1 WO 2024075042A1
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WIPO (PCT)
Prior art keywords
unit
hydrogen
gas stream
refinery
ethane
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Application number
PCT/IB2023/059972
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English (en)
Inventor
Vilas Bhagwat PATIL
Srikant Vasant BADGANDI
Original Assignee
Sabic Global Technologies B.V.
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Publication of WO2024075042A1 publication Critical patent/WO2024075042A1/fr

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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
    • C10G9/34—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
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • 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
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins

Definitions

  • the present disclosure generally relates to systems and methods for integrating petrochemical and refinery operations. More specifically, the present disclosure relates to systems and methods for collecting a hydrogen-rich gas stream generated as a byproduct or off-gas during petrochemical plant operations and supplying the hydrogen gas stream to a hydrotreatment unit or hydrocracking unit at a refinery, while also collecting an ethane-rich gas stream generated as a byproduct or off-gas during a refinery operation and supplying the ethane gas stream to an ethane steam cracker at the petrochemical plant, thereby maximizing production of olefins, such as ethylene and/or propylene, at a petrochemical plant while reducing refinery energy demand.
  • olefins such as ethylene and/or propylene
  • Hydrogen (H2) gas may be generated in situ during several petrochemical plant operations, including chlor-alkali production, ethane steam cracking, methyl tertiary butyl ether (MTBE) production, propane and butane dehydrogenation, and catalytic reforming.
  • hydrogen may be produced as a co-product together with other light gases in the form of hydrogen rich off-gas streams that typically have a hydrogen content ranging from about 80 mol% to about 90 mol%.
  • excess hydrogen-rich gas streams generated at petrochemical plants are commonly flared or wasted to the atmosphere.
  • refineries may have a hydrogen manufacturing unit (HMU) for the generation of hydrogen from natural gas (NG) feedstock.
  • HMU hydrogen manufacturing unit
  • the hydrogen generated by the HMU may be used by hydrotreating and hydrocracking operations at the refinery.
  • HMU operation at refineries is energy and feedstock intensive. Accordingly, there is a need to increase the efficiency or synergy of petrochemical and refining operations by utilizing the waste of off-gas byproducts thereby reducing overall feedstock or energy requirements.
  • Applicant has developed systems and methods for integrating or synergizing petrochemical and refinery operations so as to meet one of several operational needs, such as increased efficiency, reduction of waste, and increased economic benefit.
  • the method for integrating petrochemical and refinery operations includes the following steps: collecting a hydrogen-rich gas stream or excess hydrogen off-gas stream generated as a byproduct of a petrochemical operation at a petrochemical plant; purifying the hydrogen-rich gas stream or excess hydrogen off-gas stream to produce a purified hydrogen gas stream; supplying the purified hydrogen gas stream to a hydrotreatment unit or a hydrocracking unit at a refinery; collecting an ethane-rich gas stream generated as a byproduct of a refinery operation at the refinery; and supplying the ethane-rich gas stream to an ethane steam cracker at the petrochemical plant to produce ethylene.
  • the hydrogen-rich gas stream may be an off-gas by-product generated by the petrochemical operation and the ethane-rich gas stream may be an off-gas generated by the refinery operation.
  • substantially all of the hydrogen gas generated as a byproduct of a petrochemical operation at petrochemical plant, that would typically be wasted or flared, is collected and supplied to a hydrotreatment unit or a hydrocracking unit at refinery in order to reduce the natural gas or other energy demands of one or more refinery operations.
  • the petrochemical operation may be chlor-alkali production, ethane steam cracking, methyl tertiary butyl ether (MTBE) production, propane and butane dehydrogenation, catalytic reforming, or any combination thereof.
  • the refinery operation may include a cracking operation, such as fluid catalytic cracking.
  • the hydrogen-rich gas stream may be purified by processing the hydrogen-rich gas stream through a pressure swing adsorption unit or through a guard bed.
  • the purified hydrogen gas stream comprises 99.9 weight percent of hydrogen.
  • the purified hydrogen gas stream may contain greater than 90 wt.% hydrogen gas, or greater than 95 wt.% hydrogen gas, or greater than 98 wt.% hydrogen gas, or at least 99 wt.% hydrogen gas or at least 99.9 wt.% hydrogen gas.
  • the method may include mixing the purified hydrogen gas stream with a hydrogen gas stream produced by the hydrogen manufacturing unit at the refinery to generate a combined hydrogen gas stream.
  • the combined hydrogen gas stream may be fed to the hydrotreatment unit or the hydrocracking unit.
  • the hydrotreatment unit or the hydrocracking unit may be coupled with the hydrogen manufacturing unit.
  • the method may include reducing the demand load on a hydrogen manufacturing unit at the refinery in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit at a refinery.
  • the method may further include reducing natural gas consumption at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit.
  • the method may further include reducing carbon dioxide emission at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit.
  • Embodiments may include supplying the ethane-rich gas stream to an ethane steam cracker located at the petrochemical plant such that propylene is generated in addition to ethylene.
  • the present disclosure also provides an integrated system for petrochemical and refinery operations.
  • the system may include a petrochemical plant and a refinery unit.
  • the petrochemical plant may include a hydrogen off-gas collection unit operable to collect a hydrogen-rich gas stream generated as a byproduct of a petrochemical operation.
  • the petrochemical plant may further include a hydrogen off-gas purification unit operable to purify the hydrogen-rich gas stream to produce a purified hydrogen gas stream and an ethane steam cracker operable to receive an ethane- rich gas stream.
  • the refinery unit may include a hydrotreatment unit or a hydrocracking unit operable to receive the purified hydrogen gas stream from the hydrogen off-gas purification unit and an ethane off-gas collection unit operable to collect the ethane-rich gas stream generated as a byproduct of a refinery operation and in fluid communication with the ethane steam cracker.
  • the hydrogen-rich gas stream may be an off-gas byproduct generated by the petrochemical operation and the ethane-rich gas stream may be an offgas generated by the refinery operation.
  • the refinery operation may include a cracking operation, such as fluid catalytic cracking.
  • the petrochemical plant may further include at least one processing unit selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, and any combination thereof.
  • the petrochemical operation in the system may be a chlor-alkali production, an ethane steam cracking, a methyl tertiary butyl ether (MTBE) production, a propane and butane dehydrogenation, a catalytic reforming, or any combination thereof.
  • the at least one processing unit may be coupled to the hydrogen off-gas collection unit.
  • the hydrogen off-gas purification unit may include a pressure swing adsorption unit or one or more guard beds.
  • the purified hydrogen gas stream may contain greater than 90 wt.% hydrogen gas, or greater than 95 wt.% hydrogen gas, or greater than 98wt.% hydrogen gas, or at least 99 wt.% hydrogen gas or at least 99.9 wt.% hydrogen gas.
  • the refinery may further include a hydrogen manufacturing unit operable to produce hydrogen gas from natural gas.
  • the hydrogen manufacturing unit (HMU) may be coupled to the hydrotreatment unit or the hydrocracking unit.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream such that the demand load on the hydrogen manufacturing unit is reduced.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive a hydrogen fuel mixture comprising the purified hydrogen gas stream, or a portion thereof, and a hydrogen gas stream produced by the hydrogen manufacturing unit.
  • Embodiments of the system include a hydrotreatment unit or a hydrocracking unit operable to receive the purified hydrogen gas stream so as to reduce natural gas consumption or carbon dioxide emissions at the hydrogen manufacturing unit.
  • the ethane steam cracker is operable to produce ethylene and propylene from the ethane- rich gas stream and the ethane off-gas collection unit is operable to send ethane-rich gas stream to the ethane steam cracker at the petrochemical plant.
  • the ethane steam cracker is operable to produce ethylene and propylene from the ethane- rich gas stream and the ethane off-gas collection unit is operable to send ethane-rich gas stream to the ethane steam cracker at the petrochemical plant.
  • FIG. 1 is a graphical representation of a system for integrating petrochemical and refinery operations, according to an exemplary embodiment of the present disclosure.
  • the present disclosure describes various embodiments related to processes, methods, and systems for integrating petrochemical and refinery operations. Further embodiments may be described and disclosed.
  • the term “about” refers to a range of values including the specified value, which a person of ordinary skill in the art would consider reasonably similar to the specified value. In embodiments, “about” refers to values within a standard deviation using measurements generally acceptable in the art.. In one non-limiting embodiment, when the term “about” is used with a particular value, then “about” refers to a range extending to ⁇ 10% of the specified value, alternatively ⁇ 5% of the specified value, or alternatively ⁇ 1% of the specified value, or alternatively ⁇ 0.5% of the specified value. In embodiments, “about” refers to the specified value.
  • Disclosed here are systems and methods for integrating petrochemical and refinery operations.
  • the presently disclosed systems and methods provide for the synergistic use of off-gases as feed streams in petrochemical and refinery operations thereby maximizing light olefin production at a petrochemical plant while simultaneously reducing refinery energy demand.
  • the present disclosure involves systems and methods for collecting excess hydrogen-rich gas stream generated as a byproduct or off-gas during petrochemical plant operations and supplying the hydrogen gas stream to a hydrotreatment unit or hydrocracking unit at a refinery, while also collecting an ethane-rich gas stream generated as a byproduct or off-gas during a refinery operation and supplying the ethane gas stream to an ethane steam cracker at the petrochemical plant.
  • FIG. 1 is a schematic depicting a system 500 for integrating petrochemical and refinery operations, according to an exemplary embodiment of the present disclosure.
  • system 500 may include a petrochemical plant 100 and a refinery unit 200.
  • the petrochemical plant 100 may include one or more petrochemical operations 110 capable of generating hydrogen off-gas 105.
  • Non-limiting examples of petrochemical operations 110 may include a chlor-alkali production operation, an ethane steam cracking operation, a methyl tertiary butyl ether (MTBE) production operation, a propane and butane dehydrogenation operation, and a catalytic reforming operation.
  • MTBE methyl tertiary butyl ether
  • the one or more petrochemical operations 110 at the petrochemical plant 100 may be in the form of a processing unit 110 selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, and any combination thereof.
  • a processing unit 110 selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, and any combination thereof.
  • the processing unit 110 may be an electrified cracker which generates a substantial excess of hydrogen off-gas.
  • the electrified cracker may be employed as part of a de-carbonization strategy at the petrochemical plant.
  • the substantial excess hydrogen off-gas produced by an electrified cracker may not be useable as a fuel within the cracker complex.
  • the present disclosure provides a system 500 having improved utilization of hydrogen off-gas that increases the efficiency of system 500.
  • the petrochemical plant 100 may include a hydrogen off-gas collection unit 150 coupled to the one or more petrochemical operations 110 or processing unit 110.
  • the hydrogen off-gas collection unit 150 is operable to collect the hydrogen-rich off-gas stream 105 generated as a byproduct of the petrochemical operation 110 or operation of processing unit 110.
  • the hydrogenrich off-gas stream 105 may be contaminated with salts, chlorides, alkanes, alkenes, and other contaminants depending on the process technology deployed and the feed characteristics.
  • the presently disclosed system 500 includes a means for purifying the hydrogen-rich off-gas stream 105 so that it is suitable for utilization by hydrotreating or hydrocracking operations at a refinery.
  • the petrochemical plant 100 may further include a hydrogen off-gas purification unit 120 coupled to the hydrogen off-gas collection unit 150.
  • the hydrogen off-gas purification unit 120 is operable to purify the hydrogen-rich off-gas stream 105 collected by the hydrogen off-gas collection unit 150 to produce a purified hydrogen gas stream 125.
  • the hydrogen off-gas purification unit 120 may include a pressure swing adsorption unit and/or one or more guard beds.
  • the purified hydrogen gas stream 125 may contain greater than 90 wt.% hydrogen gas, or greater than 95 wt.% hydrogen gas, or greater than 98 wt.% hydrogen gas, or at least 99 wt.% hydrogen gas or at least 99.9 wt.% hydrogen gas.
  • petrochemical plant 100 may further include an ethane steam cracker 130 operable to receive an ethane-rich gas stream and produce light olefins 135, such as ethylene and propylene.
  • ethane steam cracker 130 operable to receive an ethane-rich gas stream and produce light olefins 135, such as ethylene and propylene.
  • the refinery unit 200 may include a hydrotreatment or hydrocracking unit 230 operable to receive a hydrogen gas stream.
  • hydrocracking unit 230 may be configured to upgrade a vacuum gasoil feedstock through cracking while injecting hydrogen gas to produce diesel or kerosene products.
  • refinery unit 200 may include a hydrogen manufacturing unit (HMU) 220 operable to produce a hydrogen gas stream 225 from natural gas, naphtha, and/or liquefied petroleum gas (LPG) feedstock 210.
  • HMU 220 is operable to receive a natural gas or fuel feed stream 215 and produce a hydrogen gas stream 225.
  • the hydrogen manufacturing unit (HMU) 220 may be coupled to the hydrotreatment unit or the hydrocracking unit 230 for the purpose of feeding a hydrogen gas stream 227 to the hydrotreatment or hydrocracking unit 230.
  • the hydrotreatment unit or the hydrocracking unit 230 is operable to receive the purified hydrogen gas stream 125 produced by the hydrogen off-gas purification unit 120 at the petrochemical plant 100 such that the demand load on the hydrogen manufacturing unit 220 is reduced. Therefore, system 500 includes a means for transporting purified hydrogen gas stream 125 from petrochemical plant 100 to hydrotreatment or hydrocracking unit 230 at refinery 200.
  • the means for transporting the purified hydrogen gas stream 125 from petrochemical plant 100 to hydrotreatment or hydrocracking unit 230 at the refinery 200 may include any known in the art, including a pipeline or vehicular transport, such as by truck or railcar, and may include any necessary intermediate facilities or storage tanks.
  • the hydrotreatment or hydrocracking unit 230 may be operable to receive a hydrogen fuel mixture 227 comprising the purified hydrogen gas stream 125 generated at the petrochemical plant 100, or a portion thereof, and a hydrogen gas stream 225 produced by the hydrogen manufacturing unit 220.
  • system 500 includes a hydrotreatment or hydrocracking unit 230 operable to receive the purified hydrogen gas stream 125 from the petrochemical plant 100 so as to reduce natural gas consumption or carbon dioxide emissions at the hydrogen manufacturing unit 220.
  • the refinery unit 200 may also include one or more refinery operations 240 capable of producing an ethane-rich off-gas stream 242.
  • the refinery operation 240 may include a cracking operation, such as fluid catalytic cracking.
  • Refinery unit 200 may further include an ethane off-gas collection unit 250 operable to collect the ethane-rich gas stream 242 generated as a byproduct of a refinery operation 240.
  • a portion 248 of the ethane-rich off-gas 245 collected by ethane off-gas collection unit may be utilized a fuel in the refinery fuel gas header.
  • a portion 247 of the ethane-rich off-gas stream 245 from ethane off-gas collection unit 250 is diverted as a feedstock to ethane cracker 130 at the petrochemical plant 100.
  • the ethane steam cracker 130 at petrochemical plant 100 is operable to receive the ethane-rich off-gas stream 247, or a portion thereof, from the ethane off-gas collection unit 250 and/or refinery operation 240 at the refinery unit 200.
  • the ethane stream cracker 130 is further operable to produce light olefins, such as ethylene and propylene, from the ethane-rich gas stream 247 received from the refinery unit 200. Therefore, system 500 includes a means for transporting the ethane-rich gas stream 245 from the ethane off-gas collection unit 250 or refinery operation 240 at refinery 200 to the ethane steam cracker 130 at petrochemical plant 100.
  • the means for transporting the ethane-rich gas stream gas stream 245 from refinery 200 to ethane steam cracker 130 at the petrochemical plant 100 may include any known in the art, including a pipeline or vehicular transport, such as by truck or railcar, and may include any necessary intermediate facilities or storage tanks.
  • the ethane off-gas collection unit 250 may be in fluid communication with the ethane steam cracker 130.
  • the ethane off-gas collection unit 250 is operable to send ethane-rich gas stream 245 to the ethane steam cracker 130 at the petrochemical plant 100.
  • the presently disclosed system 500 is operable to increase light olefin production at the petrochemical plant 100 by providing an additional ethane-rich gas stream to the ethane stream cracker 130 derived from off-gas waste generated by one or more refinery operations 240.
  • a portion of the ethane off-gas 248 from ethane off-gas collection unit 250 or refinery operation 240 may be used to supply the refinery fuel gas header.
  • a portion 217 of the natural gas and fuel feed 215 to the hydrogen manufacturing unit 220 may also be diverted to supply the fuel gas header at the refinery 200.
  • the hydrogen off-gases generated at the petrochemical plant 100, or a purified hydrogen gas stream generated therefrom may be swapped for an energetically or economically equivalent amount of ethane-rich off-gas generated by one or more refinery operations 240 at the refinery 200. In this manner, a synergism between petrochemical plant 100 operations and refinery 200 operations may be established.
  • a method for integrating petrochemical and refinery operations is illustrated by the system described in FIG. 1.
  • the method may include collecting the hydrogen-rich gas stream 105 generated as a byproduct of a petrochemical operation 110 at a petrochemical plant 100 and purifying the hydrogen-rich gas stream to produce a purified hydrogen gas stream 125.
  • the method may further include supplying the purified hydrogen gas stream 125 to a hydrotreatment unit or a hydrocracking unit 230 at a refinery 200 and collecting an ethane- rich gas stream 242 generated as a byproduct of a refinery operation 240 at the refinery 200.
  • the method may further include supplying the ethane-rich gas stream 247, or a portion thereof, to an ethane steam cracker 130 at the petrochemical plant 100 to produce light olefins such as ethylene and propylene.
  • the present disclosure provides systems and methods for the integration of petrochemical and refinery operations such that ethylene and/or propylene production is increased at a petrochemical plant while reducing energy demand at a refinery.
  • the present disclosure provides a method for integrating petrochemical and refinery operations, the method comprising: collecting excess hydrogen-rich off-gas streams generated as a byproduct of a petrochemical operation at a petrochemical plant; purifying the hydrogen-rich gas stream to produce a purified hydrogen gas stream; supplying the purified hydrogen gas stream to a hydrotreatment unit or a hydrocracking unit at a refinery; collecting an ethane-rich gas stream generated as a byproduct of a refinery operation at the refinery; and supplying the ethane-rich gas stream to an ethane steam cracker at the petrochemical plant to produce ethylene.
  • the petrochemical operation in the preceding method embodiment may be selected from the group consisting of chlor-alkali production, ethane steam cracking, methyl tertiary butyl ether (MTBE) production, propane and butane dehydrogenation, catalytic reforming, and any combination thereof.
  • MTBE methyl tertiary butyl ether
  • the hydrogen-rich gas stream may be purified by processing the hydrogen-rich gas stream through a pressure swing adsorption unit.
  • the hydrogen-rich gas stream may be purified by processing the hydrogen-rich gas stream through a guard bed.
  • the purified hydrogen gas stream may comprise at least 99.9 weight percent of hydrogen.
  • the preceding method embodiment may further include in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or a hydrocracking unit, reducing demand load on a hydrogen manufacturing unit at the refinery.
  • the preceding method embodiment may further include, prior to the step of supplying the purified hydrogen gas stream to the hydrotreatment unit or a hydrocracking unit, mixing the purified hydrogen gas stream with a hydrogen gas stream produced by the hydrogen manufacturing unit at the refinery to generate a combined hydrogen gas stream, the combined hydrogen gas stream fed to the hydrotreatment unit or the hydrocracking unit.
  • the hydrotreatment unit or the hydrocracking unit may be coupled with the hydrogen manufacturing unit.
  • the preceding method embodiment may further include, in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit, reducing natural gas consumption at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery.
  • the preceding method embodiment may further include in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit, reducing carbon dioxide emission at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery.
  • the hydrogen-rich gas stream may be an off-gas by-product generated by the petrochemical operation.
  • the refinery operation may include a cracking operation.
  • the cracking operation may be fluid catalytic cracking.
  • the ethane-rich gas stream may be an off-gas generated by the refinery operation.
  • supplying the ethane-rich gas stream to an ethane steam cracker located at the petrochemical plant may produce propylene in addition to the ethylene.
  • the present disclosure also provides an integrated system for petrochemical and refinery operations operable to increase ethylene and/or propylene production at a petrochemical plant while reducing energy demand at a refinery.
  • the integrated system for petrochemical and refinery operations may comprise: a petrochemical plant comprising: a hydrogen off-gas collection unit operable to collect a hydrogen-rich gas stream generated as a byproduct of a petrochemical operation; a hydrogen off-gas purification unit operable to purify the hydrogen-rich gas stream to produce a purified hydrogen gas stream; and an ethane steam cracker operable to receive an ethane- rich gas stream; and a refinery unit comprising: a hydrotreatment unit or a hydrocracking unit operable to receive the purified hydrogen gas stream from the hydrogen off-gas purification unit; and an ethane off-gas collection unit operable to collect the ethane-rich gas stream generated as a byproduct of a refinery operation and in fluid communication with the ethane steam cracker
  • the petrochemical operation may be chlor-alkali production, an ethane steam cracking, a methyl tertiary butyl ether (MTBE) production, a propane and butane dehydrogenation, a catalytic reforming, or any combination thereof.
  • the petrochemical plant in the preceding system embodiment may further include at least one processing unit selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, or any combination thereof, the at least one processing unit coupled to the hydrogen off-gas collection unit.
  • the hydrogen off-gas purification unit may comprise a pressure swing adsorption unit. In the preceding system embodiment, the hydrogen off-gas purification unit may comprise one or more guard beds. In the preceding system embodiment, the purified hydrogen gas stream may comprise at least 99.9 wt.% hydrogen gas.
  • the refinery in the preceding system embodiment may further comprise a hydrogen manufacturing unit operable to produce hydrogen gas from natural gas and coupled to the hydrotreatment unit or the hydrocracking unit.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream such that the demand load on the hydrogen manufacturing unit is reduced.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive a hydrogen fuel mixture, the hydrogen fuel mixture comprising the purified hydrogen gas stream, or a portion thereof, and a hydrogen gas stream produced by the hydrogen manufacturing unit.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream and reduce natural gas consumption at the hydrogen manufacturing unit.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream and reduce carbon dioxide emissions at the hydrogen manufacturing unit.
  • the hydrogen-rich gas stream may be an off-gas generated by the petrochemical operation.
  • the ethane steam cracker may be operable to produce ethylene and propylene from the ethane-rich gas stream.
  • the refinery operation may be a cracking operation.
  • the cracking operation may be fluid catalytic cracking.
  • the ethane off-gas collection unit may be operable to send the ethane-rich gas stream to the ethane steam cracker at the petrochemical plant.
  • the present disclosure also provides a method for the integration of petrochemical and refinery operations resulting in increased ethylene and/or propylene production at a petrochemical plant while reducing energy demand at a refinery.
  • the present disclosure provides a method for integrating petrochemical and refinery operations, the method comprising: collecting a hydrogen-rich gas stream generated as a byproduct of a petrochemical operation at a petrochemical plant; purifying the hydrogen-rich gas stream to produce a purified hydrogen gas stream; supplying the purified hydrogen gas stream to a hydrotreatment unit or a hydrocracking unit at a refinery; collecting an ethane-rich gas stream generated as a byproduct of a refinery operation at the refinery; and supplying the ethane-rich gas stream to an ethane steam cracker at the petrochemical plant to produce ethylene.
  • the petrochemical operation in the preceding method embodiment may be selected from the group consisting of chlor-alkali production, ethane steam cracking, methyl tertiary butyl ether (MTBE) production, propane and butane dehydrogenation, catalytic reforming, and any combination thereof.
  • the hydrogen-rich gas stream may be purified by processing the hydrogen-rich gas stream through a pressure swing adsorption unit.
  • the hydrogen-rich gas stream may be purified by processing the hydrogen-rich gas stream through a guard bed.
  • the purified hydrogen gas stream may comprise at least 99.9 weight percent of hydrogen.
  • Any of the preceding method embodiments may further include, in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or a hydrocracking unit, reducing demand load on a hydrogen manufacturing unit at the refinery.
  • Any of the preceding method embodiments may further include, prior to the step of supplying the purified hydrogen gas stream to the hydrotreatment unit or a hydrocracking unit, mixing the purified hydrogen gas stream with a hydrogen gas stream produced by the hydrogen manufacturing unit at the refinery to generate a combined hydrogen gas stream, the combined hydrogen gas stream fed to the hydrotreatment unit or the hydrocracking unit.
  • the hydrotreatment unit or the hydrocracking unit may be coupled with the hydrogen manufacturing unit.
  • any of the preceding method embodiments may further include, in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit, reducing natural gas consumption at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery. Any of the preceding method embodiments may further include in response to supplying the purified hydrogen gas stream to the hydrotreatment unit or the hydrocracking unit, reducing carbon dioxide emission at the hydrogen manufacturing unit coupled with the hydrotreatment unit or the hydrocracking unit at the refinery.
  • the hydrogen-rich gas stream may be an off-gas by-product generated by the petrochemical operation.
  • the refinery operation may include a cracking operation.
  • the cracking operation may be fluid catalytic cracking.
  • the ethane-rich gas stream may be an off-gas generated by the refinery operation.
  • supplying the ethane-rich gas stream to an ethane steam cracker located at the petrochemical plant may produce propylene in addition to the ethylene.
  • the present disclosure also provides an integrated system for petrochemical and refinery operations operable to increase ethylene and/or propylene production at a petrochemical plant while reducing energy demand at a refinery.
  • the integrated system for petrochemical and refinery operations may comprise: a petrochemical plant comprising: a hydrogen off-gas collection unit operable to collect a hydrogen-rich gas stream generated as a byproduct of a petrochemical operation; a hydrogen off-gas purification unit operable to purify the hydrogen-rich gas stream to produce a purified hydrogen gas stream; and an ethane steam cracker operable to receive an ethane- rich gas stream; and a refinery unit comprising: a hydrotreatment unit or a hydrocracking unit operable to receive the purified hydrogen gas stream from the hydrogen off-gas purification unit; and an ethane off-gas collection unit operable to collect the ethane-rich gas stream generated as a byproduct of a refinery operation and in fluid communication with the ethane steam cracker
  • the petrochemical operation may be chlor-alkali production, an ethane steam cracking, a methyl tertiary butyl ether (MTBE) production, a propane and butane dehydrogenation, a catalytic reforming, or any combination thereof.
  • MTBE methyl tertiary butyl ether
  • the petrochemical plant in any of the preceding system embodiments may further include at least one processing unit selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, or any combination thereof, the at least one processing unit coupled to the hydrogen off-gas collection unit.
  • at least one processing unit selected from the group consisting of a chlor-alkali production unit, an ethane steam cracking unit, a methyl tertiary butyl ether (MTBE) production unit, a propane and butane dehydrogenation unit, a catalytic reforming unit, or any combination thereof, the at least one processing unit coupled to the hydrogen off-gas collection unit.
  • MTBE methyl tertiary butyl ether
  • the hydrogen off-gas purification unit may comprise a pressure swing adsorption unit. In any of the preceding system embodiments, the hydrogen off-gas purification unit may comprise one or more guard beds. In any of the preceding system embodiments, the purified hydrogen gas stream may comprise at least 99.9 wt.% hydrogen gas.
  • the refinery in any of the preceding system embodiments may further comprise a hydrogen manufacturing unit operable to produce hydrogen gas from natural gas and coupled to the hydrotreatment unit or the hydrocracking unit. In any of the preceding system embodiments, the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream such that the demand load on the hydrogen manufacturing unit is reduced.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive a hydrogen fuel mixture, the hydrogen fuel mixture comprising the purified hydrogen gas stream, or a portion thereof, and a hydrogen gas stream produced by the hydrogen manufacturing unit.
  • the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream and reduce natural gas consumption at the hydrogen manufacturing unit. In any of the preceding system embodiments, the hydrotreatment unit or the hydrocracking unit may be operable to receive the purified hydrogen gas stream and reduce carbon dioxide emissions at the hydrogen manufacturing unit. In any of the preceding system embodiments, the hydrogen-rich gas stream may be an offgas generated by the petrochemical operation.
  • the ethane steam cracker may be operable to produce ethylene and propylene from the ethane-rich gas stream.
  • the refinery operation may be a cracking operation.
  • the cracking operation may be fluid catalytic cracking.
  • the ethane off-gas collection unit may be operable to send the ethane-rich gas stream to the ethane steam cracker at the petrochemical plant.
  • Implementation of the exemplary embodiment of the system provided in FIG. 1 results in a quantifiable savings of natural gas demand on the hydrogen manufacturing unit (HMU) as well as a corresponding reduction in CO2 emissions due to the decreased load on the HMU in addition to providing additional feedstock to the ethane cracker at the petrochemical plant.
  • HMU hydrogen manufacturing unit
  • implementation of the presently disclosed system produces 70 tons/day (t/d) hydrogen off-gas 105 from petrochemical plant operation 110 resulting in 56 t/d purified hydrogen gas stream 125 available to be fed to the hydrotreatment or hydrocracking unit 230 at the refinery 200.
  • the resultant reduced demand on the HMU 220 produced a natural gas savings of 90 t/d even after fulfilling the fuel gas header make-up in the refinery by natural gas.
  • implementation of the presently disclosed system and method yielded 160 t/d of ethane-rich refinery off-gas produced by refinery operation 140 that was available to be fed to the ethane cracker 130 at petrochemical plant 100. This results in a direct savings of about 90 t/d of natural gas that would otherwise be fed to the hydrogen manufacturing unit, resulting in about 200 t/d of carbon dioxide emission reductions.
  • ranges from any lower limit may be combined with any upper limit to recite a range not explicitly recited, as well as, ranges from any lower limit may be combined with any other lower limit to recite a range not explicitly recited, in the same way, ranges from any upper limit may be combined with any other upper limit to recite a range not explicitly recited.
  • reference to values stated in ranges includes each and every value within that range, even though not explicitly recited. Thus, every point or individual value may serve as its own lower or upper limit combined with any other point or individual value or any other lower or upper limit, to recite a range not explicitly recited.

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Abstract

La présente invention concerne des systèmes et des procédés d'intégration d'opérations pétrochimiques et de raffinage. Un tel procédé comprend la collecte d'un flux de gaz riche en hydrogène généré en tant que sous-produit d'une opération pétrochimique dans une usine pétrochimique et la purification du flux de gaz riche en hydrogène pour produire un flux d'hydrogène gazeux purifié. Ce procédé consiste en outre à fournir le flux d'hydrogène gazeux purifié à une unité d'hydrotraitement ou à une unité d'hydrocraquage dans une raffinerie et à collecter un flux de gaz riche en éthane généré en tant que sous-produit d'une opération de raffinage dans la raffinerie de façon que le flux de gaz riche en éthane peut être fourni à un vapocraqueur dans l'usine pétrochimique pour produire des oléfines telles que l'éthylène et le propylène.
PCT/IB2023/059972 2022-10-04 2023-10-04 Procédés et systèmes d'intégration d'opérations pétrochimiques et de raffinage WO2024075042A1 (fr)

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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130248419A1 (en) * 2012-03-20 2013-09-26 Saudi Arabian Oil Company Integrated hydroprocessing, steam pyrolysis and catalytic cracking process to produce petrochemicals from crude oil
WO2015000848A1 (fr) * 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Processus et installation pour transformer du pétrole brut en produits pétrochimiques à rendement en carbone amélioré
EP3110926A1 (fr) * 2014-02-25 2017-01-04 Saudi Basic Industries Corporation Procede d'hydrocraquage integre
US20210163832A1 (en) * 2019-12-03 2021-06-03 Saudi Arabian Oil Company Processing facility to form hydrogen and petrochemicals

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130248419A1 (en) * 2012-03-20 2013-09-26 Saudi Arabian Oil Company Integrated hydroprocessing, steam pyrolysis and catalytic cracking process to produce petrochemicals from crude oil
WO2015000848A1 (fr) * 2013-07-02 2015-01-08 Saudi Basic Industries Corporation Processus et installation pour transformer du pétrole brut en produits pétrochimiques à rendement en carbone amélioré
EP3110926A1 (fr) * 2014-02-25 2017-01-04 Saudi Basic Industries Corporation Procede d'hydrocraquage integre
US20210163832A1 (en) * 2019-12-03 2021-06-03 Saudi Arabian Oil Company Processing facility to form hydrogen and petrochemicals

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