US20150045598A1 - Flexible process for enhancing steam cracker and platforming feedstocks - Google Patents

Flexible process for enhancing steam cracker and platforming feedstocks Download PDF

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US20150045598A1
US20150045598A1 US14/260,812 US201414260812A US2015045598A1 US 20150045598 A1 US20150045598 A1 US 20150045598A1 US 201414260812 A US201414260812 A US 201414260812A US 2015045598 A1 US2015045598 A1 US 2015045598A1
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stream
passing
unit
generate
bottoms
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US14/260,812
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English (en)
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Gregory A. Funk
Steven T. Arakawa
Matthew Lippmann
Mary Jo Wier
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Honeywell UOP LLC
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UOP LLC
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Priority to US14/260,812 priority Critical patent/US20150045598A1/en
Assigned to UOP LLC reassignment UOP LLC ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FUNK, GREGORY A., ARAKAWA, STEVEN T., LIPPMANN, Matthew, WIER, MARY JO
Priority to EP14834026.8A priority patent/EP3030634B1/fr
Priority to PL14834026T priority patent/PL3030634T3/pl
Priority to KR1020167005550A priority patent/KR102318324B1/ko
Priority to PCT/US2014/037044 priority patent/WO2015020707A1/fr
Priority to CN201480054243.1A priority patent/CN105593343B/zh
Priority to TW103118856A priority patent/TWI488957B/zh
Publication of US20150045598A1 publication Critical patent/US20150045598A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/06—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural parallel stages only
    • 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
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural parallel stages only
    • 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
    • C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
    • C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
    • C10G61/04—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only the refining step being an extraction
    • 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
    • C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
    • C10G61/02—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only
    • C10G61/06—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen plural serial stages only the refining step being a sorption process
    • 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
    • C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
    • C10G61/10—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen processes also including other conversion 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
    • C10G63/00—Treatment of naphtha by at least one reforming process and at least one other conversion process
    • C10G63/06—Treatment of naphtha by at least one reforming process and at least one other conversion process plural parallel stages only
    • C10G63/08—Treatment of naphtha by at least one reforming process and at least one other conversion process plural parallel stages only including at least one 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including a sorption process as the refining step 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/16—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural parallel stages only
    • 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
    • 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
    • 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
    • C10G69/08—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 reforming naphtha
    • C10G69/10—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 reforming naphtha hydrocracking of higher boiling fractions into naphtha and reforming the naphtha obtained
    • 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
    • C10G69/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural parallel stages only
    • 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
    • C10G2400/02—Gasoline
    • 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 invention relates to a process and system for the production of aromatics from a heavier hydrocarbon stream.
  • this process provides for increasing yields and flexibility of the production of aromatics and light olefins from hydrocarbon feedstock.
  • hydrocarbon feedstreams from a raw petroleum source include the production of useful chemical precursors for use in the production of plastics, detergents and other products.
  • Processes include splitting feeds and operating several reformers using different catalysts, such as a monometallic catalyst or a non-acidic catalyst for lower boiling point hydrocarbons and bi-metallic catalysts for higher boiling point hydrocarbons.
  • catalysts such as a monometallic catalyst or a non-acidic catalyst for lower boiling point hydrocarbons and bi-metallic catalysts for higher boiling point hydrocarbons.
  • Other improvements include new catalysts, as presented in U.S. Pat. Nos. 4,677,094; 6,809,061; and 7,799,729.
  • Light olefins have traditionally been produced through the process of steam or catalytic cracking, and comprise ethylene and propylene. Light olefins are also derived from the same feedstocks as gasoline. Because of the limited availability and high cost of petroleum sources, the cost of producing light olefins from such petroleum sources has been steadily increasing. The ability to shift components in the feedstock for light olefins and gasoline pools enables producers to economically choose the most important product line and to shift some of the hydrocarbon components in an efficient manner.
  • a process for improving yields of light olefins, reformate, and providing flexibility in the processing of a naphtha feed is presented.
  • a first embodiment of the invention is a process to increase light olefin and reformate yields, comprising passing a first portion of a hydrocarbon feedstream to a fractionation column to generate an overhead stream comprising C6 compounds and lighter components, and a bottoms stream comprising heavier hydrocarbons; passing the overhead stream to a cracking unit. passing the bottoms stream to a separation unit to generate an extract stream comprising normal hydrocarbons, and a raffinate stream comprising non-normal hydrocarbons; and passing the extract stream to the cracking unit to generate light olefins.
  • a second embodiment of the invention is a process for increasing light olefin yields comprising passing a hydrocarbon stream to a fractionation column to generate a first overhead stream comprising nC4 and lighter hydrocarbons, and a first bottoms stream comprising C5 and heavier hydrocarbons; passing the first bottoms stream to a separation unit to generate an extract stream comprising normal hydrocarbons, and a raffinate stream comprising non-normal hydrocarbons; passing the raffinate stream to a reforming unit to generate a reformate stream; and passing the extract stream to a cracking unit to generate light olefins.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph further comprising passing raffinate stream to a raffinate separation system to generate a second overhead stream comprising C5 and C6 hydrocarbons, an intermediate stream comprising C7 and heavier alkanes, and C6 and heavier aromatics and naphthenes, and a second bottoms stream comprising desorbent.
  • a third embodiment of the invention is a process for providing flexibility in gasoline production passing a hydrocarbon stream to a fractionation column to generate a first overhead stream comprising nC4 and lighter hydrocarbons, and a first bottoms stream comprising C5 and heavier hydrocarbons; passing the first bottoms stream to a hydrogenation unit to generate a treated bottoms stream having a reduced acetylenes, diolefins, sulfur and nitrogen content; passing the treated bottoms stream to a separation unit to generate an extract stream comprising normal hydrocarbons, and a raffinate stream comprising non-normal hydrocarbons; passing the raffinate stream to a reforming unit to generate a reformate stream; and passing a portion of the extract stream to a cracking unit to generate light olefins.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the third embodiment in this paragraph further comprising passing the extract stream to an extract separation system to generate a second overhead stream comprising C5 and C6 normal alkanes, an intermediate stream comprising C7 and heavier normal alkanes, and a second bottoms stream comprising desorbent.
  • the process includes the use of an isomerization unit for converting a C5-C6 stream.
  • the isomerization unit can be used to convert an iC5-iC6 stream to a mixture of iC5-iC6 and normal C5 and C6 components for increasing yields of light olefins.
  • a stream of nC5-nC6 can be passed through the isomerization unit to convert the stream to a mixture of iC5-iC6 and normal C5 and C6 components for increasing the yields for a gasoline pool.
  • FIG. 1 is a base case showing the process of splitting a naphtha stream between a feed to a cracking unit and a feed to a reforming unit;
  • FIG. 2 is an embodiment showing the separation of the naphtha splitter bottoms stream to increase the light olefins yield
  • FIG. 3 is an embodiment showing the separation of the naphtha splitter bottoms stream with isomerization for increasing light olefin yields
  • FIG. 4 is an embodiment showing the separation of the naphtha splitter bottoms stream with isomerization for increasing gasoline blending pool yields.
  • a process for increasing the yields of light olefins or shifting to increase the hydrocarbon components to gasoline blending pools from a hydrocarbon feedstock.
  • the process includes separating a naphtha feedstock to components to a first stream, or a cracking unit feedstream, that are more readily processed in a cracking unit and to components in a second stream, or a reforming unit feedstream, that are more readily processed in a reforming unit.
  • the process includes the ability to convert components from the cracking stream to the reforming stream, and to convert components from the reforming stream to the cracking stream.
  • the processing of a naphtha feedstream can be used in the production of light olefins and providing hydrocarbon components for a gasoline blending pool or for reforming components to generate aromatic compounds to be passed to an aromatics complex.
  • a basic process as shown in FIG. 1 , includes splitting a naphtha feedstream into two portions, a second portion 6 , and a first portion 8 .
  • the amount of the second portion can be as little as zero, or can include all of the naphtha feedstream, depending on the choice of product.
  • the second portion 6 is passed to a cracking unit 20 for generating a process stream 22 having light olefins.
  • Light olefins include ethylene and propylene.
  • the first portion 8 of the naphtha feedstream is passed to a naphtha splitter 10 to generate an overhead stream 12 and a bottoms stream 14 .
  • the overhead stream 12 includes C6 and lighter components in the naphtha feedstream.
  • the bottoms stream 14 includes C6 and heavier components in the naphtha feedstream.
  • the typical range for the heavier components is from C5 to C11 hydrocarbons.
  • the splitter 10 operated based on the relative boiling points of the hydrocarbon components, and the splitter overhead stream 12 can comprise components that have boiling points equal to or lower than methyl cyclopentane (MCP). Operating conditions can be changed to adjust for desired overhead compositions, including changing the operating conditions to have an overhead stream 12 comprising C4 and lighter components, with the bottoms stream 14 comprising C5 and heavier components.
  • the overhead stream 12 is passed to the cracking unit 20 .
  • the bottoms stream 14 is passed to a hydrotreating unit 30 to generate a treated stream 32 .
  • the treated stream 32 is passed to a reforming unit 40 to generate a reformate stream 42 having an increased aromatics content.
  • Normal components in the hydrocarbon stream are more readily cracked to form light olefins than non-normal components.
  • the normal components are also more difficult to reform to aromatics than non-normal components.
  • branched paraffins are preferred components for a gasoline blending pool over normal components.
  • the separation of normal and non-normal components, combined with passing the different stream to appropriate downstream processing units improves flexibility and the economics of cracking and reforming naphtha.
  • the ability to convert normal components to non-normal components allows the shifting of hydrocarbon components from the stream fed to a cracking unit to a stream for generating gasoline components.
  • the process is for increasing the light olefin and reformate yields.
  • the process includes passing a first portion 8 of a hydrocarbon feedstream to a fractionation column 10 to generate an overhead stream 12 comprising C6 and lighter components, and a bottoms stream 14 comprising heavier components.
  • the overhead stream 12 is passed to a cracking unit 20 to generate a process stream 22 that includes light olefins.
  • the bottoms stream 14 is passed to a hydrotreating unit 30 to generate a treated bottoms stream 32 .
  • the hydrotreating unit 30 removes impurities to protect downstream catalysts and adsorbents. Impurities removed include sulfur compounds and nitrogen compounds.
  • the treated bottoms stream 32 is passed to a separation unit 50 to generate an extract stream 52 and a raffinate stream 54 .
  • the separation unit 50 is preferably an adsorption separation unit, and includes an adsorbent to selectively adsorb components from the treated bottoms stream.
  • the adsorbent is selected to preferentially adsorb normal components from the stream 32 , while rejecting non-normal components.
  • the extract stream 52 comprises normal hydrocarbons in the C5 to C11 range
  • the raffinate stream 54 comprises non-normal components from the bottoms stream.
  • the non-normal components include branched paraffins, naphtenes and aromatic compounds.
  • the extract stream 52 is passed to the cracking unit 20 to increase the light olefins yield from the hydrocarbon feedstream.
  • the hydrocarbon feedstream is a naphtha feedstream.
  • the present embodiment is exemplified by a naphtha feedstream, the process is not limited to a naphtha feedstream, and can include any feedstream with a composition that overlaps with a naphtha feedstream.
  • the cracking unit 20 can be a naphtha steam cracking unit.
  • the process further includes passing the raffinate stream 54 to a reforming unit 40 to generate a reformate stream 42 having an increased aromatics content.
  • the process can further include passing a second portion 6 of the hydrocarbon feedstream to the cracking unit 20 .
  • naphtha for the generation of ethylene and propylene is common It is known that normal paraffins, n-paraffins, are preferred for the relative ease of cracking over non-normal paraffins. Likewise, naphtha is used as a feedstock for reforming to generate aromatic compounds that can be used in an aromatics complex or as part of a gasoline blending pool. Non-normal paraffins are also useful components for a gasoline blending pool, or for reforming Enhancing the ability to convert a naphtha feedstock for the production of light olefins or for the production of gasoline or aromatics can enhance a refinery's economics.
  • the process provides for enhancing light olefin yields.
  • the process includes passing a hydrocarbon feedstream 8 to a fractionation unit 10 .
  • the fractionation unit 10 generates an overhead stream 12 , comprising C4 and lighter hydrocarbon components, and a bottoms stream 14 comprising C5 and heavier components.
  • the overhead stream 12 is passed to a cracking unit 20 to generate a process stream 22 having light olefins.
  • the bottoms stream 14 is passed to a hydrotreating unit 30 to generate a treated bottoms stream 32 .
  • the treated bottoms stream 32 is passed to a separation unit 50 to generate an extract stream 52 comprising normal hydrocarbons, and a raffinate stream 54 comprising non-normal hydrocarbons.
  • the non-normal hydrocarbons include branched paraffins, naphthenes and aromatics.
  • the extract stream 52 is passed to the cracking unit 20 .
  • the raffinate stream 54 is passed to a raffinate separation system 60 , and generates a raffinate overhead stream 62 , an intermediate raffinate stream 64 , and a raffinate bottoms stream 66 .
  • the separation unit 50 comprises an adsorption separation system, and includes using a desorbent as a working fluid in the adsorption separation process.
  • the raffinate bottoms stream 66 comprises the desorbent and is recycled back to the separation unit 50 .
  • the intermediate raffinate stream comprises non-normal C7 to C11 paraffins, and C6 to C11 aromatic and naphthenic components in the raffinate stream.
  • the raffinate overhead stream 62 comprises iC5 and iC6 components from the raffinate stream.
  • the raffinate overhead stream 62 is passed to an isomerization unit 70 to generate an isomerate stream 72 .
  • the isomerization unit 70 comprises a catalytic reactor that takes a mixture of hydrocarbon components and isomerizes the components to generate a new composition for the isomerate stream 72 .
  • the isomerization process can convert branched paraffins to normal paraffins, or can be used to convert normal paraffins to branched paraffins.
  • the feed to the isomerization unit consists of branched paraffins, and will generate a mixture of branched and normal paraffins.
  • the isomerate stream 72 is passed to the separation unit 50 . This embodiment increases the amount of normal paraffins generated and increases the feed to the cracking unit 20 .
  • the increase feed of normal paraffins to the cracking unit increases the amount of light olefins generated for the cracking process stream 22 .
  • the process provides for flexibility to increase gasoline production, or to increase aromatics production.
  • the process includes passing a hydrocarbon feedstream 8 to a fractionation unit 10 .
  • the fractionation unit 10 generates an overhead stream 12 , comprising C4 and lighter hydrocarbon components, and a bottoms stream 14 comprising C5 and heavier components.
  • the overhead stream 12 is passed to a cracking unit 20 to generate a process stream 22 having light olefins.
  • the bottoms stream 14 is passed to a hydrotreating unit 30 to generate a treated bottoms stream 32 .
  • the treated bottoms stream 32 is passed to a separation unit 50 to generate an extract stream 52 comprising normal hydrocarbons, and a raffinate stream 54 comprising non-normal hydrocarbons.
  • the non-normal hydrocarbons include branched paraffins and olefins, naphthenes and aromatics.
  • the raffinate stream 54 is passed to a raffinate separation system 60 , and generates a raffinate overhead stream 62 , an intermediate raffinate stream 64 , and a raffinate bottoms stream 66 .
  • the separation unit 50 comprises an adsorption separation system, and includes using a desorbent as a working fluid in the adsorption separation process.
  • the raffinate bottoms stream 66 comprises the desorbent and is recycled back to the separation unit 50 .
  • the intermediate raffinate stream comprises non-normal C7 to C11 paraffins and C6 to C11 aromatic and naphthenic components in the raffinate stream.
  • the raffinate overhead stream 62 comprises iC5 and iC6 components from the raffinate stream, which can then be passed to a gasoline blending pool, or other desired downstream process.
  • the extract stream 52 is passed to an extract separation system 80 , and generates an extract overhead stream 82 , an intermediate extract stream 84 , and an extract bottoms stream 86 .
  • the extract bottoms stream 86 comprises desorbent and is recycled to the adsorption separation unit 50 .
  • the extract intermediate stream 84 comprises C7 to C11 normal paraffins and is passed to the cracking unit 20 to generate light olefins.
  • the extract overhead stream 82 comprises nC5 and nC6 paraffins, and is passed to the isomerization unit 70 to generate an isomerization process stream 72 .
  • the isomerization process stream 72 is passed to the separation unit 10 to convert a stream of normal paraffins to a mixture of normal and branched paraffins.
  • This embodiment increases the amount of branched paraffins and increases the amount of raffinate from the separation unit 10 . This provides an increase in iC5 and iC6, and results in an increase in the raffinate overhead stream 62 , or an increase in the feed to a gasoline blending pool.
  • the extract separation system and/or the raffinate separation system can comprise one or more fractionation columns for separating the respective extract or raffinate stream into multiple streams.
  • Options for the extract separation and/or raffinate separation system include divided wall columns or other means for separating hydrocarbon streams.
  • the addition of the separation unit 10 can be seen in the following results, wherein there is a substantial increase in the normals content and aromatics content. This promotes the increase of light olefins for cracking.
  • the addition of isomerization also show that one can increase the normals and aromatics. This provides a useful enhancement of existing facilities.
  • Case 1 provides a comparison of the standard processing used in industry today, wherein a straight run naphtha is fed to a steam cracker with a minimum of preparation.
  • the straight run naphtha may be combined with light ends from a separate naphtha stream that is being process for a catalytic reforming unit.
  • the normals in the naphtha are typically in the 15% to 30% by weight range.
  • the separation unit With the addition of the separation unit, the separation can increase the amount of normals, as shown in case 2, for the feed to the cracking unit.
  • the addition of the isomerization unit allows for further improvement in the quality of feeds to the cracking unit, and to the reforming unit.
  • the quality of the feed to the reforming unit (N+2A, or aromatic potential) shows that the treatment improves yields from the reforming unit.
  • the addition of the isomerization unit also allows for more flexibility by allowing a plant operator to control the feeds to either the cracking unit or the reforming unit, but shifting the quality of the hydrocarbon stream.
  • the isomerization unit allows of increasing either the amount of normal, or the amount of branched paraffins, in the form of iC5 and iC6.

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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)
US14/260,812 2013-08-07 2014-04-24 Flexible process for enhancing steam cracker and platforming feedstocks Abandoned US20150045598A1 (en)

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US14/260,812 US20150045598A1 (en) 2013-08-07 2014-04-24 Flexible process for enhancing steam cracker and platforming feedstocks
EP14834026.8A EP3030634B1 (fr) 2013-08-07 2014-05-07 Procédé flexible d'amélioration de charges d'alimentation de vapocraqueur et de reformage au platine
PL14834026T PL3030634T3 (pl) 2013-08-07 2014-05-07 Elastyczny sposób ulepszania krakera parowego i platformowania surowców
KR1020167005550A KR102318324B1 (ko) 2013-08-07 2014-05-07 증기 분해기를 향상시키고 공급 원료를 플랫포밍하기 위한 플렉시블 공정
PCT/US2014/037044 WO2015020707A1 (fr) 2013-08-07 2014-05-07 Procédé flexible d'amélioration de charges d'alimentation de vapocraqueur et de reformage au platine
CN201480054243.1A CN105593343B (zh) 2013-08-07 2014-05-07 用于增强蒸汽裂化器及铂重整进料的灵活方法
TW103118856A TWI488957B (zh) 2013-08-07 2014-05-29 用於增加蒸汽裂解物及重組進料之彈性方法

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US14/260,812 US20150045598A1 (en) 2013-08-07 2014-04-24 Flexible process for enhancing steam cracker and platforming feedstocks

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US20220213395A1 (en) * 2021-01-07 2022-07-07 Saudi Arabian Oil Company Integrated fcc and aromatic recovery complex to boost btx and light olefin production
US11473022B2 (en) 2021-01-07 2022-10-18 Saudi Arabian Oil Company Distillate hydrocracking process with an n-paraffins separation step to produce a high octane number isomerate stream and a steam pyrolysis feedstock
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PL3030634T3 (pl) 2019-08-30
CN105593343B (zh) 2018-06-05
KR20160040645A (ko) 2016-04-14
TWI488957B (zh) 2015-06-21
TW201506147A (zh) 2015-02-16
EP3030634A1 (fr) 2016-06-15
CN105593343A (zh) 2016-05-18
KR102318324B1 (ko) 2021-10-28
EP3030634B1 (fr) 2019-02-06
WO2015020707A1 (fr) 2015-02-12

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