WO1998036037A1 - Procede d'aromatisation du naphte - Google Patents

Procede d'aromatisation du naphte Download PDF

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Publication number
WO1998036037A1
WO1998036037A1 PCT/US1998/002747 US9802747W WO9836037A1 WO 1998036037 A1 WO1998036037 A1 WO 1998036037A1 US 9802747 W US9802747 W US 9802747W WO 9836037 A1 WO9836037 A1 WO 9836037A1
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WO
WIPO (PCT)
Prior art keywords
catalyst
process recited
naphtha
modified
reforming
Prior art date
Application number
PCT/US1998/002747
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English (en)
Inventor
Jar-Lin Kao
Original Assignee
Exxon Chemical Patents Inc.
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
Priority claimed from US08/844,711 external-priority patent/US6245219B1/en
Application filed by Exxon Chemical Patents Inc. filed Critical Exxon Chemical Patents Inc.
Priority to EP98908532A priority Critical patent/EP0964903B1/fr
Priority to CA002281563A priority patent/CA2281563A1/fr
Priority to DE69819305T priority patent/DE69819305D1/de
Priority to AU66542/98A priority patent/AU6654298A/en
Publication of WO1998036037A1 publication Critical patent/WO1998036037A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used
    • C10G35/095—Catalytic reforming characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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

Definitions

  • the invention relates to a process for reforming a naphtha stream using a surface treated zeolite catalyst.
  • Naphtha streams emerging from petrochemical refining processes generally comprise a mixture of Cs to C13 hydrocarbons which include about 15 to 40 wt.% of C ⁇ to Cn aromatic compounds and the balance mostly a mixture of cs to Cn aliphatic hydrocarbons, including mixed paraffins and mixed olefins.
  • naphtha is passed over an acidic, medium pore zeolite catalyst, such as ZSM-5, which may also contain one or more dehydrogenation metals such as noble metals, under reforming conditions which include a temperature of from 400 to 1000°F (204 to 540°C), pressures of 50-300 psig, weight hourly space velocity of 0.5-25 and in the optional presence of hydrogen (H2 to oil mole ratio of about 0-10).
  • the reactions include dehydrogenation, dehydrocyclization, isomerization and hydrocracking.
  • the dehydrogenation reactions typically include dehydroisomerization of alkylcyclopentanes to aromatics, the dehydrogenation of paraffins to olefins, the dehydrogenation of cyclohexanes to aromatics and the dehydrocyclization of acyclic paraffins and acyclic olefins to aromatics.
  • the aromatization of the n-paraffins to aromatics is generally considered to be the most important because of the high octane rating of the resulting aromatic product.
  • the isomerization reactions include isomerization of n-paraffins to isoparaffins, the hydroisomerization of olefins to isoparaffins, and the isomerization of substituted aromatics.
  • the hydrocracking reactions include the hydrocracking of paraffins and hydrodesulfurization of sulfur compounds in the feed stock.
  • Acidic zeolites of the HZSM-5 type are also well known catalysts for use in toluene disproportionation reactions wherein toluene or mixtures of toluene and methanol are fed over the catalyst under disproportionation/ alkylation conditions.
  • the catalyst is first treated with a silicon-containing compound or other material to reduce the surface acidity of the catalyst. This technique has been found to enhance selectivity of the disproportionation process towards the production of the more valuable para-xylene isomers, in contrast with the meta or ortho isomers. Examples of such processes are found in U.S. Patents 4,950,835, 5,321, 183 and 5,367,099.
  • U.S. Patent 5,371,312 discloses a process for the conversion of hydrocarbons comprising passing a hydrocarbon stream over a zeolite which has been treated with an amino silane.
  • the catalyst may also contain a dehydrogenation metal such as platinum to reduce the amount of ethyl benzene by-product formed in the process.
  • U.S. Patent 5,202,513 discloses the use of a galloalumino silicate catalyst of the ZSM-5 type containing gallium as part of the crystal structure which is treated with an alkali hydroxide, used as a reforming catalyst for naphtha-type feeds.
  • WO 96/03209 discloses a reforming process wherein a C5-C9 paraffin or olefin feedstock is contacted under reforming conditions with a zeolite catalyst which has been modified with a platinum group component metal and a second metal selected from gallium, zinc, indium, iron, tin and boron.
  • the publication indicates that the process leads to an increased yield of para-xylene and that the yield of para-xylene is further enhanced by pre-coking the catalyst prior to use in the reforming process.
  • Another object of the invention is to provide a process for reforming a naphtha feed using a modified zeolite catalyst wherein the para-xylene content of the Cs aromatic product present in the reformate is produced in greater than an equilibrium-amount.
  • the present invention provides a process for reforming a naphtha hydrocarbon stream containing at least about 25 wt.% of Cs to C ⁇ aliphatic and cycloaliphatic hydrocarbons comprising contacting said stream under reforming conditions with a modified reforming catalyst comprising an intermediate pore size acidic aluminosuicate support impregnated with at least one dehydrogenation metal selected from the group consisting of gallium, zinc, indium, iron, tin and boron, and oxides or sulfides thereof, said catalyst modified by (a) contact of said impregnated aluminosilicate support with a Periodic Table Group HA metal hydroxide or an organosilicon compound in an amount sufficient to neutralize at least a portion of the acid sites present on the surface of said support and (b) calcination of said support, the reformed naphtha product of said process containing less than about 25 wt.% of C ⁇ -C 4 gas.
  • a modified reforming catalyst comprising an intermediate
  • the process of the invention provides a reformate product which on the one hand, contains a reduced content of low value Ci to C 4 gases which are primarily the by-product of cracked C 4 + aliphatic and cycloaliphatic compounds while, on the other hand, maintaining a high yield of more valuable C ⁇ to C_ aromatics in the reformate, and greater than equilibrium-amount yields of para-xylene in the Cs aromatic component of the reformate.
  • Zeolites which may be used as molecular sieve support material for the catalyst of the present invention include intermediate pore size zeolites having an average pore size in the range of about 5 to about 7 Angstroms and a Si ⁇ 2 Al 2 ⁇ 3 ratio of at least 10. These include zeolites having a MFI, MEL, TON, MTT or FER crystalline structure. Preferred such zeolites include ZSM-5, silicalite (a high silica to alumina ratio form of ZSM-5), ZSM-11, ZSM-12, ZSM-21, ZSM-22, ZSM-23, ZSM-35 and ZSM-38, with ZSM-5 being most preferred.
  • the zeolite is preferably used in its highly acidic form, e.g. HZSM-5.
  • the zeolite as synthesized, contains alkali or alkaline earth metal cations, these can be exchanged with ammonium cations, followed by calcination in air at 600°F (315°C) to 1000°F (540°C) by techniques well known in the art to produce the acid form of the zeolite.
  • the dehydrogenation metals may be incorporated into the zeolite structure by any suitable method such as impregnation (incipient wetness method) or by ion exchange.
  • the zeolite is impregnated with the metal by well known methods such as by contacting a solution of a metal salt dissolved in an aqueous or alcoholic medium with the zeolite particles for a period of time sufficient to allow the cations to penetrate the zeolite pore structure.
  • Suitable salts include the chlorides and nitrates. After drying the resulting zeolite precursor, it is preferably calcined at temperatures of from 300°C to 600°C for a period of 1 to 6 hours.
  • the metal will be present in the zeolite structure in the form of the oxide.
  • hydrogen sulfide may form under reforming conditions which may, in turn, react with the metal oxide to form at least some metal sulfide.
  • the metal may be in the form of the oxide, the sulfide or mixtures of these during the reforming process.
  • the preferred metal loading may range from about 0.1 to 10 wt.%, most preferably from about 0.5 to 5 wt.%.
  • the dehydrogenation metal present in the zeolite consists essentially of one or a mixture of gallium, zinc, indium, iron, tin or boron metal compounds, and does not contain a noble metal such as platinum, platinum/rhenium or platinum/iridium which tend to be more sensitive to deactivation by sulfur poisoning and/or coke build-up under reforming conditions.
  • a noble metal such as platinum, platinum/rhenium or platinum/iridium which tend to be more sensitive to deactivation by sulfur poisoning and/or coke build-up under reforming conditions.
  • the aluminosuicate support impregnated with the dehydrogenation metal is then modified by contact of the support with a hydroxide of a Group II A metal or an organosilicon compound in an amount sufficient to neutralize at least a portion of the acid sites present on the surface of the support, after which the catalyst is dried and calcined in air to provide the modified catalyst of this invention.
  • neutralized as used herein is intended to mean not only chemical neutralization of the support such as displacement of H + cations by alkaline earth metal ions, but also blocking of surface H + cations by silicon compounds deposited on the surface of the support and within the channels of the support.
  • the aluminosilicate support may be modified by dispersing the aluminosuicate in an about 0.1 to 2 normal aqueous solution of the hydroxide for a period of from about 0.2 to 1 hour.
  • the dispersion is heated at 25°C up to reflux temperature for a period of about 1/2 to one hour.
  • the modified aluminosilicate is separated from the solution, dried and calcined in air at a temperature of up to 1000°C, preferably from about 300°C to 600°C for a period of 1 to 24 hours.
  • Organosilicon compounds which may be used to modify the catalyst include compounds selected from the group consisting of silanes, silicones, and alkylsilicates.
  • Suitable silanes include alkoxy silanes such as tetramethoxy or tetraethyoxy silane.
  • Suitable silicones and silicone polymers include compounds having the formula -[R ⁇ R2SiO] wherein Ri and R 2 are the same or different Ci to C _ alkyl groups, phenyl groups, halogen, hydrogen, hydroxy, alkoxy, aralkyl and the like with at least one of Ri or R2 being an organic group, and n ranges from 2 to 1,000.
  • silicones examples include dimethylsilicone, copolymers of dimethylsiloxane and a lower alkylene oxide such as ethylene oxide, diethylsilicone, methyl hydrogen silicone and the like.
  • Suitable alkyl silicates include Ci to C 4 alkyl silicates such as methyl silicate or ethyl silicate.
  • the silicon compound may be deposited on the surface of the aluminosilicate by any suitable method.
  • the silicon compound may be used in liquid heat form or may be dissolved or dispersed in a solvent or aqueous medium to form a solution, dispersion or emulsion, mixed with the aluminosuicate to form a paste, dried and calcined. This deposition process can be repeated one or more times to provide a more uniformly coated product.
  • the silicon compound may be deposited on the aluminosilicate surface by well known vapor deposition techniques. The deposited silicon compound extensively covers and resides on the external surface of the aluminosilicate molecular sieve and on surfaces within the molecular sieve channels.
  • the silicon treated aluminosilicate is then calcined in air at a temperature of up to 1000°C, preferably from 300°C to 600°C, for a period of 1 to 24 hours.
  • Neutralization methods as described above should be sufficient to neutralize at least about 50%, more preferably at least about 75%, and most preferably at least about 90% of the acidic sites present on the surface of the catalyst.
  • the zeolite may be used in the catalytic process in its crystalline particulate form or it may be combined with 50 to 90 wt.%) of a binder material such a silica, alumina or various clay materials as is known in the art to form molded pellets or extrudates.
  • a binder material such as silica, alumina or various clay materials as is known in the art to form molded pellets or extrudates.
  • a zeolite-bound ZSM-5- free extrudate can also be used in the process.
  • the metal impregnation and/or silicon compound deposition process described above may be carried out before or after the zeolite is composited with the binder, preferably before.
  • the content of cracked C ⁇ -C paraffin gases produced in the naphtha reforming process of this invention is significantly lower than that produced in conventional naphtha reforming, generally less than 25 wt.% and often less than 20 wt.% of the reformate product.
  • Typical naphtha feeds which may be processed in accordance with this invention are refinery products containing at least abut 25 wt.%, more usually at least about 35 wt.%, and most usually about 50 wt.% of Cs to Co aliphatic and cycloahphatic hydrocarbons such as olefins and paraffins, about 30 to 40 wt.% of C ⁇ to C is aromatics, of which at least 5 wt.%, more usually at least 10 wt.%) constitutes C9+ aromatics and roughly 10 to 20 wt.% of which constitutes Ce-Cs aromatics (BTX).
  • These naphtha feeds may also contain 50 to 500 weight ppm sulfur and about 10 to 100 weight ppm of nitrogen compounds.
  • sulfur refers to elemental sulfur as well as sulfur compounds such as organosulfides or heterocyclic benzothiophenes.
  • Typical examples of aliphatic hydrocarbons present in the naphtha stream include paraffins such as n-hexane, 2-methylpentane, 3- methylpentane, n-heptane, 2-methylhexane, 3-methylhexane, 3- ethylpentane, 2,5-dimethylhexane, n-octane, 2-methylheptane, 3- ethylhexane, n-nonane, 2-methyloctane, 3-methyloctane and n-decane, as well as corresponding Cs to C ⁇ cyclop araffins.
  • Typical olefins include 1-hexene, 2-methyl-l-pentene, 1-heptene, 1-octene and 1- nonene.
  • Aromatics include benzene, toluene, xylenes as well as C_ to Cn aromatics.
  • the naphtha is upgraded by passing it through one or more catalyst beds positioned in a reforming reactor.
  • Suitable reforming conditions are as follows:
  • the catalyst modified in accordance with Examples 2 and 3 was prepared by impregnating 40.33 grams of calcined H+ZSM-5 powder with a solution of 2.76 grams of Zn(NOs)2 and 37.97 grams of water. After drying at 120°C for 2 hours, the catalyst precursor was calcined at 500°C for 4 hours to give a ZnO/HZSM-5 catalyst (ZnZSM-5).
  • a mixture of 20.46g of the ZnZSM-5 catalyst prepared in Example 1, 0.59g of barium hydroxide and 200 ml. of water were heated under reflux for 0.5 hour. After centrifuging, the wet solid was dried in a vacuum at 50°C for 5 hours and at 120°C for 3 hours. The dried product was pelletized to 16/45 mesh and calcined in air at 500°C for 2.5 hours to yield a barium neutralized ZnZSM-5 catalyst [BaJZnZSM- 5.
  • the catalytic test was conducted in a fixed bed at reactor 890°F, 100 psig, 2 WHSV, 2 H 2 /feed and using a Cs-221°F CAT naphtha as the feed.
  • the CAT naphtha feed contained 460 ppm sulfur, 76 ppm nitrogen, 38.1 wt.% paraffins, 11.4 wt.% cyclop araffins, 16.1 wt.% olefins and 34.4 wt.% aromatics.
  • the experimental results of these tests are as shown in Table 1.
  • coating or neutralizing the ZnZSM-5 reduced the gas make to 9.9 or 19.6 wt.%, respectively, down from 42.9 wt.% achieved using the non-modified catalyst, while maintaining a 45 to 47 wt.% aromatics yield.
  • the ZnZSM-5 catalyst from Example 1 (25.93 g) was mixed with a dimethylsiloxane-ethylene oxide copolymer (30.64 g) in neat, liquid form at room temperature for 1 hr and dried in vacuum at 60°C for 4 hr and then calcined at 530°C for 8 hr to give a one time silica coated ZnZSM-5 catalyst [i.e.(Si)ZnZSM-5]. The above procedure was repeated 3 more times to give a 4x(Si)ZnZSM-5 catalyst.
  • Example 7 The CAT naphtha used in Examples 4-6 was reformed over the non- silica containing catalyst prepared in Example 1 and the silica- containing catalyst as prepared in Example 7 under the following conditions: 50 psig, 500°C, 2 WHSV and 4 H2/molar feed ratio. Results are shown in Table 2.
  • Examples 8 and 9 were repeated except that the naphtha stream used was a fight virgin C5-C12 naphtha containing 81 wt.% paraffins and 19 wt.% of aromatics. Reforming was conducted under the following low pressure conditions: 10 psig, 527°C, 2 WHSV and 4 N2/molar feed ratio. Results are shown in Table 3.
  • Another advantage associated with the use of the catalysts of this invention as naphtha reforming catalysts is that the catalyst is more highly selective towards the production of the para-xylene component of the mixed Cs aromatics product produced of the four main Cs products, para-xylene is considerably more valuable as a chemical intermediate than ethyl benzene or the meta and ortho-xylene isomers.
  • Para-xylene occurs in approximately equilibrium amounts, about 20 to 25 wt.%, depending on the temperature, in the Cs aromatics fraction of a typical reformate stream produced using conventional noble metal- containing catalysts or using ZSM-5 catalysts modified with a dehydrogenation metal such as zinc. Reformate produced using the neutralized catalysts of this invention contains a Cs aromatic fraction which can have a content of para-xylene considerably higher than the equilibrium amount, as illustrated in Example 12 below.

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

Abstract

La présente invention concerne un procédé de réformage de courants d'alimentation en hydrocarbures contenant du naphte. Ce procédé consiste à mettre en contact un courant de naphte contenant pour environ 25 % de sa masse des hydrocarbures aliphatiques et cycloaliphatiques en C5-C9, soit avec un catalyseur de reformage tel que le ZSM-5 contenant un métal de déshydrogénation, appartenant au groupe des gallium, zinc, indium, fer, étain et bore, et qui a été modifié par contact avec un métal alcalino-terreux du groupe IIA tel que le barium, soit avec composé organosilicé, et ce, en quantité suffisante pour neutraliser au moins une partie des sites superficiels acides du catalyseur. Le réformat résultant présente une teneur réduite en gaz en C1-C4 pour une teneur accrue en para-xylène de la fraction aromatique en C8.
PCT/US1998/002747 1997-02-18 1998-02-11 Procede d'aromatisation du naphte WO1998036037A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
EP98908532A EP0964903B1 (fr) 1997-02-18 1998-02-11 Procede d'aromatisation du naphte
CA002281563A CA2281563A1 (fr) 1997-02-18 1998-02-11 Procede d'aromatisation du naphte
DE69819305T DE69819305D1 (de) 1997-02-18 1998-02-11 Naphta-aromatizationsverfahren
AU66542/98A AU6654298A (en) 1997-02-18 1998-02-11 Naphtha aromatization process

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US3540597P 1997-02-18 1997-02-18
US60/035,405 1997-02-18
US08/844,711 1997-04-18
US08/844,711 US6245219B1 (en) 1997-04-18 1997-04-18 Naphtha aromatization process

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WO1998036037A1 true WO1998036037A1 (fr) 1998-08-20

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EP (1) EP0964903B1 (fr)
KR (1) KR20000071153A (fr)
CN (1) CN1251123A (fr)
AU (1) AU6654298A (fr)
CA (1) CA2281563A1 (fr)
DE (1) DE69819305D1 (fr)
WO (1) WO1998036037A1 (fr)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002086023A1 (fr) * 2001-04-19 2002-10-31 Institut Kataliza Imeni G.K. Boreskova Sibirskogo Otdeleniya Rosiiskoi Akademii Nauk Procede de transformation des distillats de petrole
WO2016054316A1 (fr) 2014-10-03 2016-04-07 Saudi Arabian Oil Company Procédé en deux phases de production de composés aromatiques à partir de condensats de gaz de schiste/gaz naturel
US9657238B2 (en) 2014-10-03 2017-05-23 Saudi Arabian Oil Company Process for producing aromatics from wide-boiling temperature hydrocarbon feedstocks
US11001767B2 (en) 2019-04-26 2021-05-11 Exxonmobil Research And Engineering Company Naphtha reformer yield using modified zeolitic catalysts
WO2022034181A1 (fr) * 2020-08-13 2022-02-17 Haldor Topsøe A/S Procédé et installation de production d'essence à partir d'une charge contenant du goudron
CN115023286A (zh) * 2019-12-19 2022-09-06 法赫德国王石油与矿业大学 用于芳构化烃的催化剂组合物和使用该催化剂组合物生产芳族化合物的方法

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Publication number Priority date Publication date Assignee Title
US10519387B2 (en) * 2014-03-31 2019-12-31 Hindustan Petroleum Corporation Ltd. Catalyst composition for converting light naphtha to aromatic compounds and a process thereof
CN105778986B (zh) * 2016-02-23 2018-01-12 新疆恒晟能源科技股份有限公司 一种由石脑油生产混合芳烃的方法
CA3130846A1 (fr) * 2019-03-18 2020-09-24 Exxonmobil Research And Engineering Company Composes de catalyseur microporeux et leurs utilisations
EP4196555A1 (fr) * 2020-08-13 2023-06-21 Topsoe A/S Procédé et installation de production d'essence à partir d'une charge renouvelable

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WO1989004818A1 (fr) * 1987-11-17 1989-06-01 Mobil Oil Corporation Catalyseur de deshydrogenation et deshydrocyclisation, sa synthese et son utilisation
EP0361424A2 (fr) * 1988-09-29 1990-04-04 Teijin Limited Composition catalyseur, procédé pour le cracking des hydrocarbones non-aromatiques et procédé pour isomériser les hydrocarbures C-8 aromatiques
EP0530069A1 (fr) * 1991-08-23 1993-03-03 Institut Francais Du Petrole Utilisation d'un catalyseur contenant une zéolithe, un métal noble de la famille du platine et un métal additionnel dans l'aromatisation des hydrocarbures contenant de 5 à 12 atomes de carbone par molécule
US5371312A (en) * 1993-04-05 1994-12-06 Mobil Oil Corp. Shape selective hydrocarbon conversions over modified catalyst
WO1996003209A1 (fr) * 1994-07-26 1996-02-08 Chevron Chemical Company Reformage/aromatisation produisant selectivement du para-xylene

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WO1989004818A1 (fr) * 1987-11-17 1989-06-01 Mobil Oil Corporation Catalyseur de deshydrogenation et deshydrocyclisation, sa synthese et son utilisation
EP0361424A2 (fr) * 1988-09-29 1990-04-04 Teijin Limited Composition catalyseur, procédé pour le cracking des hydrocarbones non-aromatiques et procédé pour isomériser les hydrocarbures C-8 aromatiques
EP0530069A1 (fr) * 1991-08-23 1993-03-03 Institut Francais Du Petrole Utilisation d'un catalyseur contenant une zéolithe, un métal noble de la famille du platine et un métal additionnel dans l'aromatisation des hydrocarbures contenant de 5 à 12 atomes de carbone par molécule
US5371312A (en) * 1993-04-05 1994-12-06 Mobil Oil Corp. Shape selective hydrocarbon conversions over modified catalyst
WO1996003209A1 (fr) * 1994-07-26 1996-02-08 Chevron Chemical Company Reformage/aromatisation produisant selectivement du para-xylene

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002086023A1 (fr) * 2001-04-19 2002-10-31 Institut Kataliza Imeni G.K. Boreskova Sibirskogo Otdeleniya Rosiiskoi Akademii Nauk Procede de transformation des distillats de petrole
WO2016054316A1 (fr) 2014-10-03 2016-04-07 Saudi Arabian Oil Company Procédé en deux phases de production de composés aromatiques à partir de condensats de gaz de schiste/gaz naturel
US9657238B2 (en) 2014-10-03 2017-05-23 Saudi Arabian Oil Company Process for producing aromatics from wide-boiling temperature hydrocarbon feedstocks
US9957451B2 (en) 2014-10-03 2018-05-01 Saudi Arabian Oil Company Two-step process for aromatics production from natural gas/shale gas condensates
US11001767B2 (en) 2019-04-26 2021-05-11 Exxonmobil Research And Engineering Company Naphtha reformer yield using modified zeolitic catalysts
CN115023286A (zh) * 2019-12-19 2022-09-06 法赫德国王石油与矿业大学 用于芳构化烃的催化剂组合物和使用该催化剂组合物生产芳族化合物的方法
WO2022034181A1 (fr) * 2020-08-13 2022-02-17 Haldor Topsøe A/S Procédé et installation de production d'essence à partir d'une charge contenant du goudron

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EP0964903A1 (fr) 1999-12-22
KR20000071153A (ko) 2000-11-25
CN1251123A (zh) 2000-04-19
CA2281563A1 (fr) 1998-08-20
EP0964903B1 (fr) 2003-10-29
AU6654298A (en) 1998-09-08
DE69819305D1 (de) 2003-12-04

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