EP3030634B1 - Procédé flexible d'amélioration de charges d'alimentation de vapocraqueur et de reformage au platine - Google Patents

Procédé flexible d'amélioration de charges d'alimentation de vapocraqueur et de reformage au platine Download PDF

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EP3030634B1
EP3030634B1 EP14834026.8A EP14834026A EP3030634B1 EP 3030634 B1 EP3030634 B1 EP 3030634B1 EP 14834026 A EP14834026 A EP 14834026A EP 3030634 B1 EP3030634 B1 EP 3030634B1
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stream
unit
passing
generate
normal
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German (de)
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EP3030634A1 (fr
EP3030634A4 (fr
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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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    • 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 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 US Patents 4,677,094 ; 6,809,061 ; and 7,799,729 .
  • US2011245556 discloses a process for ethylene production comprising separating a naphtha boiling range feedstream in an adsorptive separation zone, steam cracking the extract stream comprising the normal paraffins and reforming the raffinate stream comprising the non-normal components.
  • 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, comprising normal and non-normal components 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; passing the extract stream to the cracking unit to generate light olefins; the process further comprising passing the raffinate stream to a reforming unit to generate a reformate stream comprising aromatics; and passing reformate stream to a reformate separation system to generate a second overhead stream comprising C5 and C6 hydrocarbons, an intermediate stream comprising C7 and
  • a process, not according to the invention, is discussed 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.
  • the process 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 process, not according to the invention, is discussed for providing flexibility in gasoline production 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 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.
  • a process 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
  • 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.
  • 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 Figure 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.
  • Figure 2 shows a process 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. In one embodiment, 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, and the raffinate stream 54 comprises non-normal components from the bottoms stream.
  • the non-normal components include branched paraffins, naphthenes 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.
  • Figure 3 shows a process 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.
  • Figure 4 shows a process for providing 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.
  • 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)

Claims (8)

  1. Procédé pour augmenter les rendements en oléfines légères et en reformat, comprenant le fait :
    de faire passer une première partie d'un courant d'alimentation en hydrocarbures, comprenant des composants normaux et anormaux dans une colonne de fractionnement pour générer un courant de tête comprenant des composés en C6 et des composants plus légers, et un courant de fond comprenant des hydrocarbures plus lourds ;
    de faire passer le courant de tête dans une unité de craquage ;
    de faire passer le courant de fond dans une unité de séparation pour générer un courant d'extrait comprenant des hydrocarbures normaux, et un courant de raffinat comprenant des hydrocarbures anormaux ;
    de faire passer le courant d'extrait dans l'unité de craquage pour générer des oléfines légères ;
    le procédé comprenant en outre le fait de faire passer le courant de raffinat dans une unité de reformage pour générer un courant de reformat comprenant des hydrocarbures aromatiques ; et
    de faire passer le courant de reformat dans un système de séparation de reformat pour générer un deuxième courant de tête comprenant des hydrocarbures en C5 et C6, un courant intermédiaire comprenant des alcanes en C7 et plus lourds, des naphtènes et des hydrocarbures aromatiques en C6 et plus lourds, et un deuxième courant de fond comprenant un désorbant.
  2. Procédé de la revendication 1, dans lequel le courant d'alimentation en hydrocarbures est le naphta.
  3. Procédé de la revendication 1, comprenant en outre le fait :
    de faire passer le courant de fond dans une unité d'hydrotraitement pour générer un courant de fond traité ; et
    de faire passer le courant de fond traité dans l'unité de séparation.
  4. Procédé de la revendication 1, dans lequel l'unité de séparation est une unité de séparation par adsorption.
  5. Procédé de la revendication 1, comprenant en outre le fait de faire passer une deuxième partie du courant d'alimentation en hydrocarbures dans l'unité de craquage.
  6. Procédé de la revendication 1, dans lequel l'unité de craquage est une unité de vapocraquage du naphta.
  7. Procédé de la revendication 1, comprenant en outre le fait de faire passer une partie du courant de raffinat dans une unité d'isomérisation pour générer un courant de procédé d'isomérisation comprenant des isoparaffines et des paraffines normales.
  8. Procédé de la revendication 7, comprenant en outre le fait de faire passer le courant de procédé d'isomérisation dans l'unité de séparation et de faire passer les paraffines normales dans l'unité de craquage.
EP14834026.8A 2013-08-07 2014-05-07 Procédé flexible d'amélioration de charges d'alimentation de vapocraqueur et de reformage au platine Active EP3030634B1 (fr)

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PL14834026T PL3030634T3 (pl) 2013-08-07 2014-05-07 Elastyczny sposób ulepszania krakera parowego i platformowania surowców

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US201361863019P 2013-08-07 2013-08-07
US14/260,812 US20150045598A1 (en) 2013-08-07 2014-04-24 Flexible process for enhancing steam cracker and platforming feedstocks
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

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WO2017196619A1 (fr) * 2016-05-11 2017-11-16 Uop Llc Utilisation de reformage catalytique au platine pour l'isomérisation des paraffines légères
US11807818B2 (en) * 2021-01-07 2023-11-07 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
US11820949B2 (en) * 2021-01-15 2023-11-21 Saudi Arabian Oil Company Apparatus and process for the enhanced production of aromatic compounds

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US5132486A (en) * 1990-10-09 1992-07-21 Wylie Engineering & Construction, Inc. Adsorption-desorption separation process for the separation of low and high octane components in virgin naphthas
US5523502A (en) * 1993-11-10 1996-06-04 Stone & Webster Engineering Corp. Flexible light olefins production
WO1999023192A1 (fr) * 1997-10-30 1999-05-14 Exxon Chemical Patents Inc. Procede de reformage du naphte
EP1063274A1 (fr) * 1999-06-17 2000-12-27 Fina Research S.A. Production d'oléfines
US20050101814A1 (en) * 2003-11-07 2005-05-12 Foley Timothy D. Ring opening for increased olefin production
KR100958362B1 (ko) * 2005-03-11 2010-05-17 유오피 엘엘씨 나프타 접촉 분해 촉매 및 방법
US7846322B2 (en) * 2005-03-11 2010-12-07 Uop Llc Integrated refinery with enhanced olefin and reformate production
FR2892126B1 (fr) * 2005-10-19 2010-04-30 Inst Francais Du Petrole Procede de conversion directe d'une charge comprenant des olefines a quatre, et/ou cinq atomes de carbone, pour la production de propylene avec une co-production d'essence desulfuree
US8283511B2 (en) * 2010-03-30 2012-10-09 Uop Llc Ethylene production by steam cracking of normal paraffins
CN105264050B (zh) * 2013-06-04 2017-12-08 环球油品公司 石脑油裂解

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EP3030634A1 (fr) 2016-06-15
CN105593343B (zh) 2018-06-05
US20150045598A1 (en) 2015-02-12
KR20160040645A (ko) 2016-04-14
TW201506147A (zh) 2015-02-16
WO2015020707A1 (fr) 2015-02-12
EP3030634A4 (fr) 2017-03-15
CN105593343A (zh) 2016-05-18
TWI488957B (zh) 2015-06-21
KR102318324B1 (ko) 2021-10-28
PL3030634T3 (pl) 2019-08-30

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