EP0964903B1 - Procede d'aromatisation du naphte - Google Patents

Procede d'aromatisation du naphte Download PDF

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Publication number
EP0964903B1
EP0964903B1 EP98908532A EP98908532A EP0964903B1 EP 0964903 B1 EP0964903 B1 EP 0964903B1 EP 98908532 A EP98908532 A EP 98908532A EP 98908532 A EP98908532 A EP 98908532A EP 0964903 B1 EP0964903 B1 EP 0964903B1
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Prior art keywords
catalyst
process recited
support
naphtha
reforming
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EP0964903A1 (fr
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Jar-Lin Kao
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ExxonMobil Chemical Patents Inc
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ExxonMobil Chemical Patents Inc
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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 C 5 to C 13 hydrocarbons which include about 15 to 40 wt.% of C 6 to C 11 aromatic compounds and the balance mostly a mixture of c 5 to C 11 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 0.345 - 2.068 MPag (50-300 psig), weight hourly space velocity of 0.5-25 and in the optional presence of hydrogen (H 2 to oil mole ratio of about 0-10).
  • an acidic, medium pore zeolite catalyst such as ZSM-5, which may also contain one or more dehydrogenation metals such as noble metals
  • the reactions include dehydrogenation, dehydrocyclization, isomerization and hydrocracking.
  • the use of a zinc-modified ZSM-5 aluminosilicate as a reforming catalyst for light naphtha feedstock is disclosed by Fukase et al, "Catalysts in Petrochemical Refining and Petrochemical Industries 1995", 1996, pp 456-464.
  • 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 C 5 -C 9 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 C 8 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 25 wt.% of C 5 to C 9 aliphatic and cycloaliphatic hydrocarbons comprising contacting said stream under reforming conditions with a modified reforming catalyst comprising an intermediate pore size acidic aluminosilicate 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 IIA 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 25 wt.% of C 1 -C 4 gas.
  • a modified reforming catalyst comprising an intermediate pore
  • the process of the invention provides a reformate product which on the one hand, contains a reduced content of low value C 1 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 6 to C 9 aromatics in the reformate, and greater than equilibrium-amount yields of para-xylene in the C 8 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 SiO 2 /Al 2 O 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.
  • 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 aluminosilicate support impregnated with the dehydrogenation metal is then modified by contact of the support with a hydroxide of a Group IIA 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 aluminosilicate 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 1 R 2 SiO] n wherein R 1 and R 2 are the same or different C 1 to C 4 alkyl groups, phenyl groups, halogen, hydrogen, hydroxy, alkoxy, aralkyl and the like with at least one of R 1 or R 2 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 C 1 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 aluminosilicate 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 1 -C 4 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 about 25 wt.%, more usually at least about 35 wt.%, and most usually about 50 wt.% of C 5 to C 9 aliphatic and cycloaliphatic hydrocarbons such as olefins and paraffins, about 30 to 40 wt.% of C 6 to C 13 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 C 6 -C 8 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 C 5 to C 9 cycloparaffins.
  • Typical olefins include 1-hexene, 2-methyl-1-pentene, 1-heptene, 1-octene and 1-nonene.
  • Aromatics include benzene, toluene, xylenes as well as C 9 to C 11 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: General Preferred Temp (°C) 204-540 427-540 Press. (MPag) [psig] 0.069-2.07 [10-300] 0.345-2.068 [50-300] WHSV 0.5-25 0.5-3 H 2 /oil mole ratio 0.10 1-10
  • 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(NO 3 ) 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 1.05 - 0.37 mm (16/45 mesh) and calcined in air at 500°C for 2.5 hours to yield a barium neutralized ZnZSM-5 catalyst [Ba]ZnZSM-5.
  • the catalytic test was conducted in a fixed bed at reactor 476.7°C (890°F), 0.689 MPag (100 psig), 2 WHSV, 2 H 2 /feed and using a C 5 - 105°C (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.% cycloparaffins, 16.1 wt.% olefins and 34.4 wt.% aromatics.
  • the experimental results of these tests are as shown in Table 1. ⁇ % Yield at 21 hr ⁇ EX CATALYST FEED CONV.
  • 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 4 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: 0.345 MPag (50 psig), 500°C, 2 WHSV and 4 H 2 /molar feed ratio. Results are shown in Table 2. Yield (wt.%) at 21 hr Example Catalyst A 6 A 7 A 8 A 9 A 10 Olefins C 5 -C 9 C 1 -C 4 8 ZnZSM-5 8.7 25.0 19.9 4.7 1.1 2.7 3.1 34.8 9 4x(Si)Zn ZSM-5 6.4 23.4 19.7 3.7 1.8 9.8 11.7 23.5
  • Examples 8 and 9 were repeated except that the naphtha stream used was a light virgin C 5 -C 12 naphtha containing 81 wt.% paraffins and 19 wt.% of aromatics. Reforming was conducted under the following low pressure conditions: 0.069 MPag (10 psig), 527°C, 2 WHSV and 4 H 2 /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 C 8 aromatics product produced of the four main C 8 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 C 8 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 C 8 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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Claims (14)

  1. Procédé de reformage d'un courant de naphta contenant au moins 25 % en poids d'hydrocarbures aliphatiques et cycloaliphatiques en C5 à C9, comprenant la mise en contact dudit courant dans des conditions de reformage avec un catalyseur de reformage modifié, comprenant un support consistant en aluminosilicate acide de diamètre des pores intermédiaire imprégné d'au moins un métal de déshydrogénation choisi dans le groupe consistant en le gallium, le zinc, l'indium, le fer, l'étain et le bore et leurs oxydes ou sulfures, ledit catalyseur étant modifié par (a) contact dudit support consistant en aluminosilicate imprégné avec un hydroxyde de métal du Groupe IIA du Tableau Périodique ou un composé organique de silicium en quantité suffisante pour neutraliser au moins une partie des sites acides présents à la surface dudit support et (b) calcination dudit support, le produit consistant en naphta reformé dudit procédé contenant moins de 25 % en poids de gaz en C1 à C4.
  2. Procédé selon la revendication 1, dans lequel ledit support consistant en aluminosilicate comprend une zéolite possédant une structure cristalline MFI, MEL, TON, MTT ou FER.
  3. Procédé selon la revendication 1 ou 2, dans lequel ledit support consistant en aluminosilicate est une zéolite ZSM-5.
  4. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit métal de déshydrogénation est le zinc.
  5. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit catalyseur est modifié par contact avec un hydroxyde de métal du Groupe IIA.
  6. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit support consistant en aluminosilicate est combiné avec un liant choisi dans le groupe consistant en la silice, l'alumine, l'argile ou une zéolite, pour former des pastilles de catalyseur.
  7. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit métal du Groupe IIA est choisi dans le groupe constitué du baryum, du calcium et du magnésium.
  8. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit catalyseur est modifié par contact avec un composé organique de silicium.
  9. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit composé organique de silicium est choisi dans le groupe constitué de silanes, silicones et silicates d'alkyle.
  10. Procédé selon l'une quelconque des revendications précédentes, dans lequel au moins 50 % des sites acides présents à la surface dudit support sont neutralisés.
  11. Procédé selon l'une quelconque des revendications précédentes, dans lequel lesdites conditions de reformage comprennent une température de 205 à 540 °C, une pression de 0,069 à 2,07 MPag (10 à 300 psig), une vitesse spatiale horaire pondérale de 0,5 à 25 et un rapport molaire entre hydrogène et hydrocarbure de 0 à 10.
  12. Procédé selon l'une quelconque des revendications précédentes, dans lequel ledit courant de naphta contient au moins 35 % en poids desdits hydrocarbures aliphatiques et cycloaliphatiques en C5 à C9.
  13. Procédé selon l'une quelconque des revendications précédentes, dans lequel le produit consistant en naphta reformé dudit procédé contient moins de 20 % en poids de gaz en C1 à C4.
  14. Procédé selon l'une quelconque des revendications précédentes, dans lequel le produit consistant en naphta reformé dudit procédé contient un produit aromatique en C8 contenant au moins 25 % en poids de plus que la quantité à l'équilibre de paraxylène.
EP98908532A 1997-02-18 1998-02-11 Procede d'aromatisation du naphte Expired - Lifetime EP0964903B1 (fr)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
US3540597P 1997-02-18 1997-02-18
US35405P 1997-02-18
US08/844,711 US6245219B1 (en) 1997-04-18 1997-04-18 Naphtha aromatization process
US844711 1997-04-18
PCT/US1998/002747 WO1998036037A1 (fr) 1997-02-18 1998-02-11 Procede d'aromatisation du naphte

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EP0964903A1 EP0964903A1 (fr) 1999-12-22
EP0964903B1 true EP0964903B1 (fr) 2003-10-29

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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)

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RU2181750C1 (ru) * 2001-04-19 2002-04-27 Институт катализа им. Г.К. Борескова СО РАН Способ переработки нефтяных дистиллятов (варианты)
WO2015150881A1 (fr) * 2014-03-31 2015-10-08 Hindustan Petroleum Corporation Ltd. Catalyseur de conversion de naphta léger en composés aromatiques
SG11201702318RA (en) 2014-10-03 2017-04-27 Saudi Arabian Oil Co Process for producing aromatics from wide-boiling temperature hydrocarbon feedstocks
JP6481026B2 (ja) 2014-10-03 2019-03-13 サウジ アラビアン オイル カンパニー 天然ガス／シェールガスコンデンセートからの芳香族生産のための２ステッププロセス
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
CN113646081B (zh) * 2019-03-18 2024-01-09 埃克森美孚科技工程公司 中孔催化剂化合物及其用途
US11001767B2 (en) 2019-04-26 2021-05-11 Exxonmobil Research And Engineering Company Naphtha reformer yield using modified zeolitic catalysts
US11439991B2 (en) * 2019-12-19 2022-09-13 King Fahd University Of Petroleum & Minerals Catalyst compositions for aromatizing hydrocarbons and processes for producing aromatic compounds using the catalyst compositions
KR20230051170A (ko) * 2020-08-13 2023-04-17 토프쉐 에이/에스 타르-함유 원료로부터 가솔린을 제조하기 위한 방법 및 플랜트
AU2021325367A1 (en) * 2020-08-13 2023-02-23 Topsoe A/S Process and plant for producing gasoline from a renewable feed

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CN1251123A (zh) 2000-04-19
DE69819305D1 (de) 2003-12-04
CA2281563A1 (fr) 1998-08-20
AU6654298A (en) 1998-09-08
KR20000071153A (ko) 2000-11-25
WO1998036037A1 (fr) 1998-08-20
EP0964903A1 (fr) 1999-12-22

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