WO2017196501A1 - Isomérisation de configuration de flux dans l'unité de reformage - Google Patents

Isomérisation de configuration de flux dans l'unité de reformage Download PDF

Info

Publication number
WO2017196501A1
WO2017196501A1 PCT/US2017/028099 US2017028099W WO2017196501A1 WO 2017196501 A1 WO2017196501 A1 WO 2017196501A1 US 2017028099 W US2017028099 W US 2017028099W WO 2017196501 A1 WO2017196501 A1 WO 2017196501A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
naphtha
passing
aromatics
paragraph
Prior art date
Application number
PCT/US2017/028099
Other languages
English (en)
Inventor
Gregory A. Funk
Jr. Ernest J. Boehm
Mary Jo Wier
Original Assignee
Uop Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uop Llc filed Critical Uop Llc
Publication of WO2017196501A1 publication Critical patent/WO2017196501A1/fr
Priority to US16/051,208 priority Critical patent/US20180334623A1/en

Links

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
    • 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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • 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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/065—Catalytic reforming characterised by the catalyst used containing crystalline zeolitic molecular sieves, other than aluminosilicates
    • 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
    • C10G63/02—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial stages only
    • C10G63/04—Treatment of naphtha by at least one reforming process and at least one other conversion process plural serial 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/302—Viscosity
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
    • 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

Definitions

  • the present invention relates to a process for the production of light olefins from a naphtha feed stream and the production of gasoline components from the naphtha feed.
  • This invention also relates to an improved flow process for increasing the yields of light olefins or shifting operations to increase gasoline production.
  • Ethylene and propylene, light olefin hydrocarbons with two or three atoms per molecule, respectively, are important chemicals for use in the production of other useful materials, such as polyethylene and polypropylene.
  • Polyethylene and polypropylene are two of the most common plastics found in use today and have a wide variety of uses for both as a material fabrication and as a material for packaging.
  • Other uses for ethylene and propylene include the production of vinyl chloride, ethylene oxide, ethylbenzene and alcohol.
  • Steam cracking or pyrolysis of hydrocarbons produces essentially all of the ethylene and propylene.
  • Hydrocarbons used as feedstock for light olefin production include natural gas, petroleum liquids, and carbonaceous materials including coal, recycled plastics or any organic material.
  • An ethylene plant is a very complex combination of reaction and gas recovery systems.
  • the feedstock is charged to a cracking zone in the presence of steam at effective thermal conditions to produce a pyrolysis reactor effluent gas mixture.
  • the pyrolysis reactor effluent gas mixture is stabilized and separated into purified components through a sequence of cryogenic and conventional fractionation steps.
  • a typical ethylene separation section of an ethylene plant containing both cryogenic and conventional fractionation steps to recover an ethylene product with a purity exceeding 99.5% ethylene is described in an article by V. Kaiser and M. Picciotti, entitled, "Better Ethylene Separation Unit.” The article appeared in HYDROCARBON PROCESSING MAGAZINE, November 1988, pages 57-61 and is hereby incorporated by reference.
  • the hydrocarbon feedstream to the zeolitic catalyst typically contains a mixture of 40 to 95 wt-% paraffins having 4 or more carbon atoms per molecule and 5 to 60 wt-% olefins having 4 or more carbon atoms per molecule.
  • the preferred catalyst for such a zeolitic cracking process is an acid zeolite, examples includes several of the ZSM-type zeolites or the borosilicates. Of the ZSM-type zeolites, ZSM-5 was preferred.
  • zeolites containing materials which could be used in the cracking process to produce ethylene and propylene included zeolite A, zeolite X, zeolite Y, zeolite ZK-5, zeolite ZK-4, synthetic mordenite, dealuminized mordenite, as well as naturally occurring zeolites including chabazite, faujasite, mordenite, and the like. Zeolites which were ion-exchanged to replace alkali metal present in the zeolite were preferred. Preferred cation exchange cations were hydrogen, ammonium, rare earth metals and mixtures thereof.
  • European Patent No. 109,059B1 discloses a process for the conversion of a feedstream containing olefins having 4 to 12 carbon atoms per molecule into propylene by contacting the feedstream with a ZSM-5 or a ZSM-11 zeolite having a silica to alumina atomic ratio less than or equal to 300 at a temperature from 400 to 600°C.
  • the ZSM-5 or ZSM-11 zeolite is exchanged with a hydrogen or an ammonium cation.
  • the reference also discloses that, although the conversion to propylene is enhanced by the recycle of any olefins with less than 4 carbon atoms per molecule, paraffins which do not react tend to build up in the recycle stream.
  • the reference provides an additional oligomerization step wherein the olefins having 4 carbon atoms are oligomerized to facilitate the removal of paraffins such as butane and particularly isobutane which are difficult to separate from C 4 olefins by conventional fractionation.
  • a process is disclosed for the conversion of butenes to propylene. The process comprises contacting butenes with a zeolitic compound selected from the group consisting of silicalites, boralites, chromosilicates and those zeolites ZSM-5 and ZSM-11 in which the mole ratio of silica to alumina is greater than or equal to 350. The conversion is carried out at a temperature from 500 to 600°C.
  • the European Patent 109060B1 discloses the use of silicalite-1 in an ion-exchanged, impregnated, or co-precipitated form with a modifying element selected from the group consisting of chromium, magnesium, calcium, strontium and barium.
  • the heavier olefins having six or more carbon atoms per molecule which are produced in commercial ethylene plants are useful for the production of aromatic hydrocarbons.
  • Portions of the olefin product include olefins with four carbon atoms per molecule. This portion includes both mono-olefins and di-olefins and some paraffins, including butane and iso-butane. Because the portion with four carbon atoms per molecule is generally less valuable and requires significant processing to separate di-olefins from the mono-olefins, processes are sought to improve the utilization of this portion of the ethylene plant product and enhancing the overall yield of ethylene and propylene.
  • reformulated gasoline include lower vapor pressure, lower final boiling point, increased oxygenate content, and lower content of olefins and aromatics.
  • Aromatics in particular benzene and toluene, have been the principal source of increasing the octane of gasoline with the removal of lead compounds, but now the aromatics content may eventually be reduced to less than 25% in major urban areas and to even lower ranges, such as less than 15%, in areas having severe pollution problems.
  • Alternate formulations for gasolines have been comprising aliphatic-rich compositions in order to maintain the octane ratings, as refiners have worked to reduce the aromatic and olefin content of gasolines.
  • the processes for increasing the aliphatic content of gasolines include the isomerization of light naphtha, isomerization of paraffins, upgrading of cyclic naphthas, and increased blending of oxygenates.
  • oxygenates are also becoming an issue as the use of methyl tertiary-butyl ether (MTBE) is being phased out, and ethanol has become the primary oxygenate for use with gasoline.
  • MTBE methyl tertiary-butyl ether
  • a process is presented for the flexible operation of the conversion of a naphtha feedstream to higher value products from either a cracking unit, or the generation of a stream for blending with a gasoline pool.
  • a first embodiment of the invention is a process for increasing light olefin yields from naphtha, comprising passing a naphtha feedstream to a naphtha splitter to generate a light naphtha stream and a heavy naphtha stream, wherein the naphtha splitter is operated to split the naphtha stream around the boiling point of methylcyclopentane; passing the heavy naphtha stream to a reforming unit to generate a reformer effluent comprising aromatics; passing the light naphtha 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 a cracking unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the boiling point of cyclohexane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the boiling point of dimethylpentane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the reformer effluent to an aromatics recovery unit to generate an aromatics stream and a recovery unit raffinate stream.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the recovery unit raffinate stream to the separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the separation unit is an adsorption separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the adsorption separation unit uses a light desorbent.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the light desorbent is n-butane or n-pentane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the raffinate stream to a gasoline blending pool.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics raffinate stream to the cracking unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics raffinate stream to the separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics stream to an aromatics complex.
  • a second embodiment of the invention is a process for increasing gasoline blending stock from naphtha, comprising passing a naphtha feedstream to a naphtha splitter to generate a light naphtha stream and a heavy naphtha stream, wherein the naphtha splitter is operated to split the naphtha stream around the boiling point of methylcyclopentane; passing the heavy naphtha stream to a reforming unit to generate a reformer effluent comprising aromatics; passing the light naphtha stream to a separation unit to generate an extract stream comprising normal hydrocarbons and a raffinate stream comprising non-normal
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter includes a side draw stream.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter is operated to send iC5 and iC4 into the overhead stream, further comprising passing the raffinate splitter overhead stream to the reformer to isomerize the iC5 and iC4 components to nC5 and nC4.
  • 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 the reformer effluent stream to an aromatics recovery unit to generate an aromatics stream and an aromatics raffinate stream.
  • 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 the aromatics raffinate stream to the separation unit to recover normal paraffins.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the adsorption separation unit uses a light desorbent.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter is operated to send iC5, cyclopentane, iC6 and methylcyclopentane into the side draw stream.
  • 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 the side draw stream to a gasoline blending stock.
  • 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 the raffinate splitter bottom stream to the reforming unit to convert
  • Figure 1 is a flow diagram for increasing the steam cracker feed and to increase the yields of light olefins; and [0017] Figure 2 is a flow diagram for increasing the production of gasoline blending components.
  • the present invention is a process that improves flexibility in the operation of a refinery, and enables the refiner to readily shift product with minimal additional equipment.
  • the operation of the new and existing equipment allows for shifting of production to increase higher value products as the market shifts.
  • Market shifts include the price of raw materials, or oil, and the demand for different products such as precursor materials to plastics, such as light olefins or aromatics, or increased production of gasoline blending streams.
  • Traditional processing of a naphtha feedstream is to only use the naphtha splitter, which segregates according to boiling point ranges.
  • the present invention is a process for increasing light olefin yields from a naphtha feedstream.
  • the naphtha feedstream 8 is passed to a naphtha splitter 10 to generate a light naphtha stream 12 and a heavy naphtha stream 14.
  • the naphtha splitter 10 is operated to split the naphtha stream around the normal boiling point of
  • the heavy naphtha stream 14 is passed to a reforming unit 40 to generate a reformer effluent stream 42 comprising aromatics.
  • the light naphtha stream 12 is passed to a separation unit 20 to generate an extract stream 22 comprising normal hydrocarbons and a raffinate stream 24 comprising non-normal hydrocarbons.
  • the extract stream 22 is passed to a cracking unit 30 to generate a cracking process stream 32 comprising light olefins.
  • the raffinate stream 24 is passed to the reforming unit 40.
  • the separation unit 20 is an adsorption separation unit, and uses a light desorbent to displace the adsorbed normal paraffins.
  • the light desorbent is selected from hydrocarbons that have a boiling point lower than the components in the light naphtha stream 12.
  • the light desorbent can comprise a light normal paraffin, such as n- butane, or n-pentane.
  • the process further includes passing the reformer effluent stream 42 to an aromatics recovery unit 50 to generate an aromatics stream 52 and an aromatics recovery unit raffinate stream 54.
  • the aromatics stream 52 is passed to an aromatics complex 60.
  • the recovery unit raffinate stream 54 comprises iso and normal hydrocarbons, and in one embodiment, is passed to the cracking unit 30. In an alternate embodiment, the recovery unit raffinate stream 54 is passed to the separation unit 20.
  • the raffinate stream 54 is passed to the separation unit 20, it may be first hydrotreated, or passed to a hydrotreatment unit 80, before being passed to the separation unit 20.
  • the hydrotreatment unit 80 can be used to hydrogenate olefins, or facilitate the removal of any sulfur that is obtained from the aromatics recovery unit 50.
  • the separation unit 20 separates the normal paraffins for passage to the cracking unit, and the non-normal hydrocarbons, and in particular the isobutane, isopentanes and isohexanes, are passed to the reforming unit 40.
  • the reforming catalyst will isomerize the iso-paraffins, and will increase the amount of normal paraffins that can be sent to the cracking unit 20.
  • the invention is a process for increasing the content for a gasoline blending pool from the naphtha feedstream.
  • the naphtha splitter 10 is operated to increase the temperature to split the naphtha stream around the normal boiling point of cyclohexane, or around 81°C.
  • the naphtha splitter 10 can also be operated at conditions to have the split around the normal boiling point of dimethylpentanes, or a temperature greater than 80°C, or in the range of 80°C to 90°C.
  • the present invention includes the processing of a naphtha feedstream to improve the feed to a steam cracker, or to improve the feed to a reforming unit, and to improve the composition of a gasoline blending stock.
  • the present invention is presented in the form wherein the temperatures are temperatures for a fractionation process operated at, or near, atmospheric pressures. The invention is intended to include appropriate shifts in temperatures for changes in operating pressures.
  • hydrocarbons would readily understand and know the temperature shifts for fractionation at either higher or lower pressures.
  • the boiling points are expected to rise for operations with increased pressures, and to drop for operations with decreased pressures, relative to atmospheric pressure.
  • the raffinate stream 24 from the separation unit 20 is passed to a second fractionation column 70 to generate a second fractionation overhead stream 72, and a second fractionation bottoms stream 76.
  • the second fractionation column 70 can have a side draw stream 74.
  • the second fractionation column 70 can be a divided wall column, or is intended to include a two column system for producing the three streams.
  • the raffinate stream 24 can be passed to the gasoline blending pool.
  • either the second overhead stream 72 or the side draw stream 74 comprise gasoline components for passing to the gasoline pool.
  • the second bottoms stream 76 is passed to the reformer 40, to aromatize cyclohexane, and to isomerize iso- paraffins.
  • the process is directed to increasing the selection of hydrocarbons for passing to a gasoline blending pool.
  • the process includes passing a naphtha feed stream 8 to a naphtha splitter 10 to generate a light naphtha stream 12 and a heavy naphtha stream 14.
  • the heavy naphtha stream 14 is passed to a reforming unit 40 to generate a reformer effluent 42.
  • the light naphtha stream 12 is passed to a separation unit 20 to generate an extract stream 22 and a raffinate stream 24.
  • the extract stream 22 comprising normal hydrocarbons, and the raffinate stream 24 comprising non- normal hydrocarbons.
  • the extract stream 22 is passed to a cracking unit 30.
  • the raffinate stream 24 includes iso-paraffins, and naphthenes that are removed from the light naphtha stream 12.
  • the raffinate stream 24 can also include some benzene. The amount of benzene will be subject to the operating conditions of the naphtha splitter 10.
  • the reformer effluent stream 42 is passed to an aromatics recovery unit 50 to generate an aromatics stream 52 and a recovery unit raffinate stream 54.
  • the aromatics stream 52 is passed to an aromatics complex 60.
  • the recovery raffinate stream 54 is passed to the separation unit 20.
  • the reformer 40 isomerizes a portion of the reformer feed 14 that is not aromatized.
  • the separation unit 20 further separates the aromatics raffinate stream 54 to direct normal hydrocarbons to the extract stream 22 and non-normal hydrocarbons to the raffinate stream 24.
  • the recovered non-normal hydrocarbons are directed to a gasoline blending pool.
  • a first embodiment of the invention is a process for increasing light olefin yields from naphtha, comprising passing a naphtha feedstream to a naphtha splitter to generate a light naphtha stream and a heavy naphtha stream, wherein the naphtha splitter is operated to split the naphtha stream around the normal boiling point of methylcyclopentane; passing the heavy naphtha stream to a reforming unit to generate a reformer effluent comprising aromatics; passing the light naphtha 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 a cracking unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the normal boiling point of cyclohexane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the naphtha splitter is operated increasing the temperature to split the naphtha stream around the normal boiling point of dimethylpentane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the reformer effluent to an aromatics recovery unit to generate an aromatics stream and a recovery unit aromatics raffinate stream.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the recovery unit raffinate stream to the separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the separation unit is an adsorption separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the adsorption separation unit uses a light desorbent.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph wherein the light desorbent is n-butane or n-pentane.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the raffinate stream to a gasoline blending pool.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics raffinate stream to the cracking unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics raffinate stream to the separation unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the first embodiment in this paragraph further comprising passing the aromatics stream to an aromatics complex.
  • a second embodiment of the invention is a process for increasing gasoline blending stock from naphtha, comprising passing a naphtha feedstream to a naphtha splitter to generate a light naphtha stream and a heavy naphtha stream, wherein the naphtha splitter is operated to split the naphtha stream around the normal boiling point of methylcyclopentane; passing the heavy naphtha stream to a reforming unit to generate a reformer effluent comprising aromatics; passing the light naphtha stream to a separation unit to generate an extract stream comprising normal hydrocarbons and a raffinate stream comprising non- normal hydrocarbons; passing the raffinate to a raffinate splitter to generate a raffinate splitter bottoms stream and a raffinate splitter overhead stream; and passing the extract stream to a cracking unit.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter includes a side draw stream.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter is operated to send iC5 and iC4 into the overhead stream, further comprising passing the raffinate splitter overhead stream to the reformer to isomerize the iC5 and iC4 components to nC5 and nC4.
  • 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 the reformer effluent stream to an aromatics recovery unit to generate an aromatics stream and an aromatics raffinate stream.
  • 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 the aromatics raffinate stream to the separation unit to recover normal paraffins.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the adsorption separation unit uses a light desorbent.
  • An embodiment of the invention is one, any or all of prior embodiments in this paragraph up through the second embodiment in this paragraph wherein the raffinate splitter is operated to send iC5, cyclopentane, iC6 and methylcyclopentane into the side draw stream.
  • 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 the side draw stream to a gasoline blending stock.
  • 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 the raffinate splitter bottom stream to the reforming unit to convert methylcyclopentane and heavier components to aromatics.

Landscapes

  • 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)
  • Crystallography & Structural Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Un procédé est présenté dans le but de récupérer les composés d'hydrocarbures présents dans une charge d'alimentation, le naphta, afin de les faire passer dans un mélange d'essence ou afin de modifier les opérations pour augmenter la production d'oléfines légères. Le procédé comprend la séparation de la charge d'alimentation, soit le naphta, en un flux de naphta léger et un flux de naphta lourd. Le procédé consiste en outre à séparer le flux de naphta léger pour récupérer des hydrocarbures non normaux de haute qualité, et à séparer les hydrocarbures normaux de la charge d'alimentation vers l'unité de craquage.
PCT/US2017/028099 2016-05-11 2017-04-18 Isomérisation de configuration de flux dans l'unité de reformage WO2017196501A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US16/051,208 US20180334623A1 (en) 2016-05-11 2018-07-31 Flow configurations using a normal paraffin separation unit with isomerization in the reforming unit

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201662334938P 2016-05-11 2016-05-11
US62/334,938 2016-05-11

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US16/051,208 Continuation US20180334623A1 (en) 2016-05-11 2018-07-31 Flow configurations using a normal paraffin separation unit with isomerization in the reforming unit

Publications (1)

Publication Number Publication Date
WO2017196501A1 true WO2017196501A1 (fr) 2017-11-16

Family

ID=60266709

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2017/028099 WO2017196501A1 (fr) 2016-05-11 2017-04-18 Isomérisation de configuration de flux dans l'unité de reformage

Country Status (2)

Country Link
US (1) US20180334623A1 (fr)
WO (1) WO2017196501A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021082578A1 (fr) * 2019-10-30 2021-05-06 中国石油化工股份有限公司 Procédé et système de traitement d'un produit de réaction de craquage catalytique, et utilisation associée

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11377609B2 (en) 2019-10-30 2022-07-05 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating hydrodealkylation and naphtha reforming
US11091708B2 (en) 2019-10-30 2021-08-17 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating selective hydrogenation and ring opening
US20210130717A1 (en) * 2019-10-30 2021-05-06 Saudi Arabian Oil Company System and process for steam cracking and pfo treatment integrating selective hydrogenation, selective hydrocracking and naphtha reforming
US11220640B2 (en) * 2019-10-30 2022-01-11 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating selective hydrogenation, FCC and naphtha reforming
US11220637B2 (en) 2019-10-30 2022-01-11 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating selective hydrogenation and FCC
US11390818B2 (en) 2019-10-30 2022-07-19 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating hydrodealkylation
US11091709B2 (en) 2019-10-30 2021-08-17 Saudi Arabian Oil Company System and process for steam cracking and PFO treatment integrating selective hydrogenation, ring opening and naphtha reforming
US11021422B1 (en) 2019-12-04 2021-06-01 Saudi Arabian Oil Company Integrated processes to produce gasoline blending components from light naphtha

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4181599A (en) * 1978-10-23 1980-01-01 Chevron Research Company Naphtha processing including reforming, isomerization and cracking over a ZSM-5-type catalyst
US20140357914A1 (en) * 2013-06-04 2014-12-04 Uop Llc Naphtha cracking
US20150045597A1 (en) * 2013-08-07 2015-02-12 Uop Llc Integrated process for gasoline or aromatics production

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6552242B1 (en) * 2001-09-07 2003-04-22 Uop Llc Fractionation in light paraffin isomerization process
US7119239B2 (en) * 2002-06-19 2006-10-10 Exxonmobil Chemical Patents Inc. Manufacture of xylenes using reformate
WO2006063201A1 (fr) * 2004-12-10 2006-06-15 Bhirud Vasant L Craquage a la vapeur avec desaromatisation de naphtha
US7514590B1 (en) * 2005-03-11 2009-04-07 Uop Llc Isomerization process with adsorptive separation
US8753503B2 (en) * 2008-07-24 2014-06-17 Uop Llc Process and apparatus for producing a reformate by introducing isopentane
EP2243814A1 (fr) * 2009-04-23 2010-10-27 Total Petrochemicals Research Feluy Amélioration de naphte léger pour améliorer la production d'oléfines
US8692046B2 (en) * 2011-01-13 2014-04-08 Uop Llc Process for isomerizing a feed stream including one or more C4-C6 hydrocarbons

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4181599A (en) * 1978-10-23 1980-01-01 Chevron Research Company Naphtha processing including reforming, isomerization and cracking over a ZSM-5-type catalyst
US20140357914A1 (en) * 2013-06-04 2014-12-04 Uop Llc Naphtha cracking
US20150045597A1 (en) * 2013-08-07 2015-02-12 Uop Llc Integrated process for gasoline or aromatics production

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2021082578A1 (fr) * 2019-10-30 2021-05-06 中国石油化工股份有限公司 Procédé et système de traitement d'un produit de réaction de craquage catalytique, et utilisation associée

Also Published As

Publication number Publication date
US20180334623A1 (en) 2018-11-22

Similar Documents

Publication Publication Date Title
US20180334623A1 (en) Flow configurations using a normal paraffin separation unit with isomerization in the reforming unit
US8137533B2 (en) Mixture of catalysts for cracking naphtha to olefins
RU2664543C2 (ru) Способы и системы для получения ароматических соединений из углеводородов каталитического крекинга
US9328299B2 (en) Naphtha cracking
US9938207B2 (en) Upgrading paraffins to distillates and lube basestocks
US20210277316A1 (en) Process for increasing the concentration of normal hydrocarbons in a stream
US20180327675A1 (en) Use of platforming process to isomerize light paraffins
WO2016102247A1 (fr) Procédé de production d'hydrocarbures c2 et c3
US8524962B2 (en) Use of olefin cracking to produce alkylate
EP3237581B1 (fr) Procédé de production d'hydrocarbures c2 et c3
CN112980502A (zh) 通过催化裂化和蒸汽裂化生产轻质烯烃的装置和方法
US9328298B2 (en) Naphtha cracking
KR102454266B1 (ko) 고비점 탄화수소 공급원료를 보다 저비점의 탄화수소 생성물로 전환하는 방법
US20180340125A1 (en) Flow control to meet e70 gasoline specifications
EP3004291B1 (fr) Craquage de naphta
IL35865A (en) High octane gasoline production
RU2747931C1 (ru) Способ увеличения выхода жидкого углеводородного продукта
EP3237583B1 (fr) Procédé de production de gpl et btx
CN112980497A (zh) 通过催化裂解生产轻质烯烃和芳族化合物的装置和方法
EP3237582B1 (fr) Procédé de production de gpl et btx
WO2023022828A1 (fr) Métathèse de c4/c5 en propylène et 1-hexène

Legal Events

Date Code Title Description
NENP Non-entry into the national phase

Ref country code: DE

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 17796542

Country of ref document: EP

Kind code of ref document: A1

122 Ep: pct application non-entry in european phase

Ref document number: 17796542

Country of ref document: EP

Kind code of ref document: A1