WO2013028160A1 - Procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures - Google Patents

Procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures Download PDF

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Publication number
WO2013028160A1
WO2013028160A1 PCT/US2011/048480 US2011048480W WO2013028160A1 WO 2013028160 A1 WO2013028160 A1 WO 2013028160A1 US 2011048480 W US2011048480 W US 2011048480W WO 2013028160 A1 WO2013028160 A1 WO 2013028160A1
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WO
WIPO (PCT)
Prior art keywords
zone
gas stream
net gas
isomerization
hydrocarbons
Prior art date
Application number
PCT/US2011/048480
Other languages
English (en)
Inventor
David James SCHECTERLE
William YANEZ
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
Priority to RU2013157344/04A priority Critical patent/RU2013157344A/ru
Priority to MYPI2013003787A priority patent/MY160208A/en
Priority to SG2013079330A priority patent/SG194628A1/en
Priority to CN201180071723.5A priority patent/CN103619787A/zh
Priority to PCT/US2011/048480 priority patent/WO2013028160A1/fr
Priority to BR112013028031A priority patent/BR112013028031A2/pt
Priority to KR1020137035148A priority patent/KR20140017685A/ko
Publication of WO2013028160A1 publication Critical patent/WO2013028160A1/fr
Priority to ZA2013/08385A priority patent/ZA201308385B/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
    • C07C5/27—Rearrangement of carbon atoms in the hydrocarbon skeleton
    • C07C5/2767—Changing the number of side-chains
    • C07C5/277—Catalytic processes
    • 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
    • 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
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/42—Hydrogen of special source or of special composition
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates generally to methods for isomerizing and reforming of hydrocarbons, and more particularly relates to methods for recovering hydrogen from isomerizing and reforming of hydrocarbons.
  • a hydrocarbon feedstock of, for example, C 5 hydrocarbons to about Cii hydrocarbons is contacted with a reforming catalyst to convert at least a portion of the heavier hydrocarbons to aromatic hydrocarbons to increase the octane content of gasoline.
  • the catalytic reforming of the heavier hydrocarbons also produces significant quantities of hydrogen, which has become very important to many refiners and can be used, for example, for hydrotreating to reduce sulfur levels in gasoline and other fuels.
  • many refineries use catalytic reforming processes that have a re-contacting zone for sequestering hydrogen from the reforming zone effluent. Unfortunately, the quantities of hydrogen that are typically recovered in catalytic reforming processes are often insufficient to meet the hydrogen demands in many refineries.
  • a light hydrocarbon fraction containing normal paraffins of, for example, butane, pentane, and/or hexane is contacted with an
  • the isomerization product stream contains branched paraffins, such as iso-butane, branched pentane, and/or branched hexane that are used to increase the octane content of gasoline.
  • the isomerization net gas stream contains hydrogen and light end hydrocarbons, e.g., Ci to C 5 and possibly some C 6 hydrocarbons. Unfortunately, many refineries burn the isomerization net gas stream as fuel gas because the equipment and operating cost associated with recovering hydrogen from this stream is prohibitively high despite their unmet need for hydrogen.
  • a method for recovering hydrogen from isomerizing and reforming of hydrocarbons comprises combining a HCl-scrubbed, isomerization-zone net gas stream that comprises hydrogen and C 6 - hydrocarbons with a reforming-zone net gas stream that comprises hydrogen and C 6 - hydrocarbons to form a combined net gas stream that comprises hydrogen and light end hydrocarbons.
  • the light end hydrocarbons are extracted from the combined net gas stream in a re-contacting zone using a reforming-zone product stream that comprises C 5 + hydrocarbons to form a hydrogen-rich net gas stream.
  • a method for recovering hydrogen from isomerizing and reforming of hydrocarbons comprises contacting a paraffin feed stream with a chloride-promoted isomerization catalyst in the presence of hydrogen to form an isomerization reactor-zone effluent.
  • the isomerization reactor-zone effluent is separated into an isomerization-zone product stream that comprises branched paraffins and a isomerization-zone net gas stream that comprises hydrogen, chloride-containing compounds including HC1, and C 6 - hydrocarbons.
  • At least a portion of the chloride-containing compounds is removed from the isomerization-zone net gas stream to form an HCl-scrubbed, isomerization-zone net gas stream.
  • Water is removed from the HCl-scrubbed, isomerization-zone net gas stream to form a water- depleted, HCl-scrubbed, isomerization-zone net gas stream.
  • the water-depleted, HCl- scrubbed, isomerization-zone net gas stream is combined with a reforming-zone net gas stream that comprises hydrogen and C 6 - hydrocarbons to form a combined net gas stream that comprises hydrogen and light end hydrocarbons.
  • the combined net gas stream is compressed with a compressor that is upstream from a re-contacting zone to form a compressed combined net gas stream.
  • the compressed combined net gas stream and a reforming-zone product stream that comprises C5+ hydrocarbons including aromatics are advanced through the re-contacting zone.
  • the light end hydrocarbons are extracted from the compressed combined net gas stream in the re-contacting zone using the reforming- zone product stream to form a hydrogen-rich net gas stream and an aromatics-containing product stream.
  • a method for recovering hydrogen from isomerizing and reforming of hydrocarbons comprises contacting a paraffin feed stream with a chloride-promoted isomerization catalyst in the presence of hydrogen to form an isomerization reactor-zone effluent.
  • the isomerization reactor-zone effluent is separated into an isomerization-zone product stream that comprises branched paraffins and a isomerization-zone net gas stream that comprises hydrogen, chloride-containing including HC1, and C 6 - hydrocarbons.
  • At least a portion of the chloride-containing compounds is removed from the isomerization-zone net gas stream to form an HCl-scrubbed, isomerization-zone net gas stream.
  • Water is removed from the HCl-scrubbed, isomerization-zone net gas stream to form a water-depleted, HCl-scrubbed, isomerization-zone net gas stream.
  • the water-depleted, HCl-scrubbed, isomerization-zone net gas stream is combined with a reforming-zone net gas stream that comprises hydrogen and C 6 - hydrocarbons in a re-contacting zone to form a combined net gas stream that comprises hydrogen and light end hydrocarbons.
  • the combined net gas stream is compressed with a compressor that is in the re-contacting zone to form a compressed combined net gas stream.
  • a reforming-zone product stream that comprises C5+ hydrocarbons including aromatics is introduced to the re-contacting zone.
  • the light end hydrocarbons is extracted from the compressed combined net gas stream in the re- contacting zone using the reforming-zone product stream to form a hydrogen-rich net gas stream and an aromatics-containing product stream.
  • FIG. 1 schematically illustrates an apparatus including a paraffin isomerization section and a hydrocarbon reforming section in accordance with an exemplary
  • FIG. 2 schematically illustrates a paraffin isomerization section of the apparatus depicted in FIG. 1;
  • FIG. 3 schematically illustrates a hydrocarbon reforming section of the apparatus depicted in FIG. 1;
  • FIG. 4 schematically illustrates a re-contacting zone of the hydrocarbon reforming section depicted in FIG. 3.
  • Various embodiments contemplated herein relate to methods for recovering hydrogen from isomerizing and reforming of hydrocarbons. Unlike the prior art, the exemplary embodiments taught herein combine an isomerization-zone net gas stream from a paraffin isomerization section with a reforming-zone net gas stream from a hydrocarbon reforming section. Prior to combining the two streams, the isomerization-zone net gas stream is scrubbed to remove chloride-containing compounds including HCl to protect the downstream equipment.
  • the reforming-zone net gas stream comprises hydrogen and C 6 - hydrocarbons and the isomerization-zone net gas stream comprises hydrogen and C 6 or lighter hydrocarbons.
  • C x means hydrocarbon molecules that have "X” number of carbon atoms
  • C x + means hydrocarbon molecules that have “X” and/or more than “X” number of carbon atoms
  • C x - means hydrocarbon molecules that have “X” and/or less than “X” number of carbon atoms.
  • C x and lighter and hydrocarbons means hydrocarbon molecules having "X” and less than "X” number of carbon atoms.
  • the two streams combine to form a combined net gas stream that comprises hydrogen and light end hydrocarbons.
  • the combined net gas stream is compressed via a compressor in the hydrocarbon reforming section to form a compressed combined net gas stream.
  • the compressed combined net gas stream is passed through a re-contacting zone of the hydrocarbon reforming section.
  • the light end hydrocarbons are extracted from the combined net gas stream using a reforming-zone product stream that comprises C 5 + hydrocarbons to form a hydrogen-rich net gas stream.
  • Overall hydrogen recovery is improved for isomerizing and reforming of hydrocarbons because the hydrogen-rich net gas stream includes hydrogen not only from the reforming-zone net gas stream but also from the isomerization-zone net gas stream.
  • the additional hydrogen recovered from the paraffin isomerization section is preferably accomplished with minimal additional equipment and cost because the hydrogen extracted from the isomerization-zone net gas stream is done using the hydrocarbon reforming section's existing equipment and re-contacting zone.
  • the apparatus 10 comprises a paraffin isomerization section 12 and a hydrocarbon reforming section 14.
  • the paraffin isomerization section 12 is utilized for a paraffin isomerization process that converts normal paraffins to branched paraffins.
  • the paraffin isomerization section 12 comprises a reaction zone 18 and a stabilizing-scrubbing zone 20.
  • the hydrocarbon reforming section 14 is utilized for a hydrocarbon reforming process that converts a C5 to Cn hydrocarbon feedstock into an aromatics-containing reformate for gasoline.
  • FIG. 2 is a detailed illustration of the paraffin isomerization section 12 in accordance with an exemplary embodiment.
  • the reaction zone 18 and the stabilizing- scrubbing zone 20 include a reactor 22 and a distillation column 24, respectively, that are in fluid communication.
  • a paraffin feed 26 is passed through a dryer 28 for removing water and to form a dried paraffin feed 29.
  • the paraffin feed 26 is rich in C 4 hydrocarbons, such as n-butane and may also contain relatively small amounts of iso-butane, pentane, and heavier materials.
  • the paraffin feed 26 is rich in C 5 and/or C 6 hydrocarbons, such as normal pentane and normal hexane.
  • a hydrogen-containing gas feed 30 is passed through a dryer 32 for removing water and is combined with the dried paraffin feed 29 to form a combined stream 34.
  • the combined stream 34 is passed through a heat exchanger 36 and a heater 38, and is introduced to the reactor 22.
  • the reactor 22 is a fixed-bed catalytic reactor operating at a temperature of about 90 to about 210°C and contains a high-activity chloride-promoted catalyst that is effective to isomerize the normal paraffins to branched paraffins (e.g., iso-butane, branched pentane, branched hexane, or combinations thereof) to produce an isomerization reaction-zone effluent 40.
  • the isomerization reaction-zone effluent 40 contains the branched paraffins, other hydrocarbons, and chloride-containing compounds including HC1.
  • the isomerization reaction-zone effluent 40 is passed through the heat exchanger 36 and is cooled to a temperature of from about 65 to about 150°C.
  • the isomerization reaction-zone effluent 40 then is introduced to the distillation column 24.
  • the distillation column 24 separates the isomerization reaction-zone effluent 40 into an isomerization product stream 42 and a liquefied petroleum gas (LPG) stream 44.
  • LPG liquefied petroleum gas
  • the isomerization product stream 42 contains branched paraffins.
  • a portion of the isomerization product stream 42 may be passed through a heater 45, heated to about 140 to about 200°C, and recycled back to the distillation column 24.
  • the LPG stream 44 is passed through a cooler 46, cooled down to about 0 to about 55°C, and is introduced to a vent drum 48.
  • a liquid stream 50 is removed from the vent drum 48 and is passed through a pump 52 to the distillation column 24 for reflux.
  • the isomerization-zone net gas stream 54 is rich in hydrogen and also contains some C 6 or lighter hydrocarbons, and chloride-containing compounds including HC1.
  • the isomerization-zone net gas stream 54 is vented from the vent drum 48 at a pressure of from about 1,000 to about 2,000 kPa.
  • the isomerization-zone net gas stream 54 is passed through a scrubber 56 to remove at least a portion of the chloride-containing compounds including HC1 to form a HCl-scrubbed, isomerization-zone net gas stream 58 that contains water absorbed from the scrubber 56.
  • the HCl-scrubbed, isomerization-zone net gas stream 58 is passed through a drying zone 59 that contains one or more dryers to remove water and form a water- depleted, HCl-scrubbed, isomerization-zone net gas stream 60. As illustrated in FIG. 1, the water-depleted, HCl-scrubbed, isomerization-zone net gas stream 60 is introduced to the hydrocarbon reforming section 14.
  • a reforming-zone feedstock 62 containing from C 5 to about Cn hydrocarbons with a boiling point range of, for example, from about 80 to about 205°C is introduced to a combined feed exchanger 64.
  • the combined feed exchanger 64 operates to exchange heat between a reforming-zone effluent 66 and the reforming-zone feedstock 62.
  • a heated reforming- zone feed stream 68 is withdrawn from the combined feed exchanger 64 and is passed through a heater 70, which is capable of interstage heating of multiple streams, to form a fully heated reforming-zone feed stream 72.
  • the fully heated reforming-zone feed stream 72 is passed to a first stage of a reforming reactor 74 that contains a reforming catalyst as is well known in the art.
  • the reforming reactor 74 is configured for continuous catalyst regeneration where spent catalyst is continuously removed from the reforming reactor 74 via line 76 and passed to a regeneration zone 78 for regeneration. Regenerated catalyst from the regeneration zone 78 is introduced into the reforming reactor 74 via line 80.
  • a reaction mixture is conducted from the reforming reactor 74 to the heater 70 and then the heated reaction mixture is returned to the reforming reactor 74.
  • a reforming-zone effluent 66 is formed in the reforming reactor 74 and contains hydrogen, a product comprising C 5 + hydrocarbons including aromatics, and lighter hydrocarbons.
  • the reforming-zone effluent 66 is passed along to the combined feed exchanger 64 where heat from the reforming-zone effluent 66 is exchanged with the reforming-zone feedstock 62 to form a partially cooled reforming- zone effluent 82.
  • the partially cooled reforming-zone effluent 82 is passed through a cooler 84 and introduced to a reforming-zone product separator 86.
  • the reforming-zone product separator 86 separates the reforming-zone effluent into a reforming zone product stream 88 comprising C5+ hydrocarbons, and a reforming-zone net gas stream 90 comprising hydrogen and C 6 - hydrocarbons.
  • Conditions for operating the reforming-zone product separator include pressures of from about 241 to about 1,400 kPa.
  • the reforming-zone net gas stream 90 is divided into a first portion 92 that is passed through a recycle compressor 94 to combine with the reforming-zone feedstock 62, and a second portion 96 that is passed along to a suction vessel 98 for a first stage net gas compressor 100.
  • the first stage net gas compressor 100 is upstream from a re-contacting zone 102.
  • the water-depleted, HCl-scrubbed, isomerization zone net gas stream 60 is combined with the reforming-zone net gas stream 90 to form a combined net gas stream that comprises hydrogen and light end hydrocarbons, such as C 5 - hydrocarbons and possibly some C 6 hydrocarbons.
  • the water-depleted, HCl- scrubbed, isomerization zone net gas stream 60 is combined with the reforming-zone net gas stream 90 and the combined net gas stream is introduced to the first stage net gas compressor 100 via the suction vessel 98 to form a compressed gas stream 104.
  • the compressed gas stream 104 preferably has a pressure of from about 1,000 to about 3,000 kPa and is introduced to the re-contacting zone 102 for further separation.
  • the reforming-zone product stream 88 is introduced to the re-contacting zone 102 and is combined with a compressed gas stream 106 to form a combined stream 109.
  • the compressed gas stream 106 is formed from a gas stream 107 from a first stage re-contacting drum 110 after being passed through the second stage compressor 108.
  • the gas stream 107 is formed from the reforming-zone net gas stream 90 or the combined net gas stream (i.e. combined net gas streams 90 and 60) and accordingly, is hydrogen rich with some low end hydrocarbons, such as C 5 - hydrocarbons.
  • the compressed gas stream 106 preferably has a pressure of from about 3,000 to about 6,000 kPa.
  • the combined stream 109 is passed through a heat exchanger 112 to adjust the temperature to about -15 to about 52°C and is introduced to a second stage re-contacting drum 114.
  • the liquid from the reforming-zone product stream 88 extracts low end hydrocarbons from the gas stream 107 to form a hydrogen-rich net gas stream 116 and a first-contacted, reforming-zone product stream 118.
  • the first-contacted, reforming-zone product stream 118 is combined with the compressed gas stream 104 to form a combined stream 120.
  • the combined stream 120 is passed through a heat exchanger 122 to adjust the temperature to about -15 to about 52°C and is introduced to the first stage re-contacting drum 110.
  • the liquid from the first-contacted, reforming-zone product stream 118 extracts low end hydrocarbons from the combined net gas stream to form the gas stream 107 and an aromatics-containing effluent 124.
  • the hydrogen-rich net gas stream 116 may optionally be passed through a chloride treater 126 to remove any chloride-containing compounds.
  • the combined net gas stream is formed in the re- contacting zone 102, such as, for example, between the first stage re-contacting drum 110 and the second stage compressor 108.
  • the water-depleted, HCl-scrubbed, isomerization zone net gas stream 60 may be passed along line 61 and combined with the reforming-zone net gas stream 90 downstream from the first stage re-contacting drum 110 but upstream from the second stage compressor 108 to form the gas stream 107.
  • the gas stream 107 is compressed in the second stage compressor 108, combined with the reforming-zone product stream 88, and introduced to the second stage re-contacting drum 114 to form the hydrogen-rich net gas stream 116.
  • the aromatics-containing effluent 124 is passed through a heat exchanger 132 to adjust the temperature to about 93 to about 204°C and is introduced to a reforming-zone stabilizer 128.
  • the reforming-zone stabilizer 128 removes light end hydrocarbons from the aromatics-containing effluent 124 to form a stabilized aromatics-containing reformate 130 that is passed through the heat exchanger 132, and a light ends gas stream 134.
  • the exemplary embodiments taught herein combine an isomerization-zone net gas stream from a paraffin isomerization section with a reforming-zone net gas stream from a hydrocarbon reforming section.
  • the reforming-zone net gas stream comprises hydrogen and C 6 - hydrocarbons and the isomerization-zone net gas stream comprises hydrogen and C 6 or lighter hydrocarbons.
  • the two streams combine to form a combined net gas stream that comprises hydrogen and light end hydrocarbons.
  • the combined net gas stream is compressed via a compressor in the hydrocarbon reforming section to form a compressed combined net gas stream.
  • the compressed combined net gas stream is passed through a re-contacting zone of the hydrocarbon reforming section.
  • the light end hydrocarbons are extracted from the combined net gas stream using a reforming-zone product stream that comprises C5+ hydrocarbons to form a hydrogen-rich net gas stream.
  • Overall hydrogen recovery is improved for isomerizing and reforming of hydrocarbons because the hydrogen-rich net gas stream includes hydrogen not only from the reforming-zone net gas stream but also from the isomerization-zone net gas stream.
  • the additional hydrogen recovered from the paraffin isomerization section is preferably accomplished with minimal additional equipment and cost because the hydrogen extracted from the isomerization-zone net gas stream is done using the hydrocarbon reforming section's existing equipment and re-contacting zone.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne, selon plusieurs modes de réalisation, des procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures. Ledit procédé comprend les étapes consistant à combiner un flux de gaz, issu de la zone d'isomérisation, débarrassé de son HCl et contenant de l'hydrogène et des hydrocarbures en C6, avec un flux de gaz issu de la zone de reformage contenant de l'hydrogène et des hydrocarbures en C6, afin d'obtenir un flux de gaz combiné contenant de l'hydrogène et des fractions légères d'hydrocarbures. Lesdites fractions légères d'hydrocarbures sont extraites du flux de gaz combiné contenant de l'hydrogène dans une zone de remise en contact utilisant un flux de produit issu de la zone de reformage contenant des hydrocarbures en C5 et plus, pour obtenir un flux de gaz riche en hydrogène.
PCT/US2011/048480 2011-08-19 2011-08-19 Procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures WO2013028160A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
RU2013157344/04A RU2013157344A (ru) 2011-08-19 2011-08-19 Способы извлечения водорода в процессе изомеризации и риформинга углеводородов
MYPI2013003787A MY160208A (en) 2011-08-19 2011-08-19 Methods for recovering hydrogen from isomerizing and reforming of hydrocarbons
SG2013079330A SG194628A1 (en) 2011-08-19 2011-08-19 Methods for recovering hydrogen from isomerizing and reforming of hydrocarbons
CN201180071723.5A CN103619787A (zh) 2011-08-19 2011-08-19 从烃的异构化和重整中回收氢气的方法
PCT/US2011/048480 WO2013028160A1 (fr) 2011-08-19 2011-08-19 Procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures
BR112013028031A BR112013028031A2 (pt) 2011-08-19 2011-08-19 método para recuperar hidrogênio de isomerização e reforma de hidrocarbonetos
KR1020137035148A KR20140017685A (ko) 2011-08-19 2011-08-19 탄화수소의 이성질화 및 개질화로부터 수소를 회수하는 방법
ZA2013/08385A ZA201308385B (en) 2011-08-19 2013-11-07 Methods for recovering hydrogen from isomerizing and reforming of hydrocarbons

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Application Number Priority Date Filing Date Title
PCT/US2011/048480 WO2013028160A1 (fr) 2011-08-19 2011-08-19 Procédés de recueil d'hydrogène impliquant l'isomérisation et le reformage d'hydrocarbures

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KR (1) KR20140017685A (fr)
CN (1) CN103619787A (fr)
BR (1) BR112013028031A2 (fr)
MY (1) MY160208A (fr)
RU (1) RU2013157344A (fr)
SG (1) SG194628A1 (fr)
WO (1) WO2013028160A1 (fr)
ZA (1) ZA201308385B (fr)

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Publication number Priority date Publication date Assignee Title
WO2016094264A3 (fr) * 2014-12-12 2016-08-04 Uop Llc Procédés intégrés et des systèmes de reformage et d'isomérisation d'hydrocarbures

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KR20140017685A (ko) 2014-02-11
ZA201308385B (en) 2015-03-25
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BR112013028031A2 (pt) 2019-09-24
MY160208A (en) 2017-02-28
RU2013157344A (ru) 2015-06-27

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