EP2631282A1 - Procédé de production de distillats intermédiaires - Google Patents

Procédé de production de distillats intermédiaires Download PDF

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Publication number
EP2631282A1
EP2631282A1 EP12382067.2A EP12382067A EP2631282A1 EP 2631282 A1 EP2631282 A1 EP 2631282A1 EP 12382067 A EP12382067 A EP 12382067A EP 2631282 A1 EP2631282 A1 EP 2631282A1
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EP
European Patent Office
Prior art keywords
naphtha
stream
process according
catalyst
alkylation
Prior art date
Legal status (The legal status 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 status listed.)
Granted
Application number
EP12382067.2A
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German (de)
English (en)
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EP2631282B1 (fr
Inventor
Iñigo Ribas Sanguesa
Rafael Roldán Mesa
Juan Pedro GÓMEZ MARTÍN
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Repsol SA
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Repsol SA
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Priority to EP12382067.2A priority Critical patent/EP2631282B1/fr
Priority to ES12382067.2T priority patent/ES2541052T3/es
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/20—Organic compounds not containing metal atoms
    • C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
    • C10G69/12—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step
    • C10G69/123—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one polymerisation or alkylation step alkylation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
    • 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
    • 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 producing middle distillates.
  • the process produces hydrogen, gasoline and middle distillate from a heavy naphtha and an olefinic stream.
  • Catalytic reforming units are catalytic units with several reactors in series, where a straight run naphtha or a conversion naphtha, such as, for example, an FCC (Fluid Catalytic Cracking) naphtha, undergoes naphthene dehydrogenation, paraffin isomerisation and paraffin dehydrocyclisation reactions, in order to improve the properties of said naphthas as fuels and, more specifically, increase their octane number for gasolines.
  • a straight run naphtha or a conversion naphtha such as, for example, an FCC (Fluid Catalytic Cracking) naphtha
  • FCC Fluid Catalytic Cracking
  • patent WO 00/39253 discloses the improvement of the cetane number of FCC heavy naphthas or FCC light gas oil, by directly alkylating them with olefinic streams, in the presence of a solid acid catalyst.
  • Patent US 4594143 discloses the alkylation of Jet-fuel (150°C-260°C) with an olefinic stream, to produce a diesel fuel fraction, using a solid acid catalyst.
  • Patent US 290460 discloses the production of alkyl aromatics with a high octane number in the gasoline distillation range, starting from aromatic and olefinic streams.
  • diesel fuel is produced from the alkylation of a direct distillation naphtha with a high aromatic content and FCC naphthas with an acid catalyst such as aluminum chloride.
  • Patent WO 2008/043066 discloses a process for the production of middle distillates, such as kerosene and diesel fuel.
  • the process includes a step where the paraffinic naphtha is converted into benzene and olefins, and the benzene and the olefins are made react, in order to obtain alkylbenzenes.
  • the process described uses a Sn/Pt catalyst to perform the first step. In said step, the production of aromatics is practically limited to benzene, since the rest of the C7+ paraffins are basically converted into olefins.
  • the present invention relates to a process to produce hydrogen, gasoline and a middle distillate which can be used for the blending of middle distillates dedicated to fuels.
  • the process can be implemented from scratch, it can be also implemented by modifying an existing catalytic reforming plant, by using one of the multiple reforming reactors for the dehydrogenation of naphthenes and the remaining reactors to carry out an alkylation process.
  • the process as herein disclosed produces hydrogen, gasoline and a middle distillate.
  • the process can also produce a LPG fraction.
  • Another advantage of the process is that it can be used as raw material olefinic streams and straight run naphthas, whose current destination is the production of gasoline or the chemical industry.
  • hydrogen is obtained, which is currently a necessary and expensive chemical and refineries may present a deficit of it.
  • the possibility of adapting a catalytic reforming plant for the production of a middle distillate from an aromatic and/or a naphthenic stream and an olefinic stream entails a reduction of the costs.
  • the catalyst of the process can be regenerated in situ by burning the coke formed during the process with air.
  • a process for producing hydrogen, gasoline and a middle distillate comprising at least the following steps:
  • a separation of benzene and a light fraction can be carried out between steps (i) and (ii).
  • Preferred heavy naphtha to be used in step (i) is an hydrocarbon stream with a content of at least 20% w/w of naphthenes plus aromatics, and with a distillation range between 75°C to 200°C, preferably between 90°C to 140 °C.
  • suitable naphtha for the process as herein disclosed are straight-run naphtha, heart cut FCC naphtha, aromatic concentrates, coker naphtha, visbreaker naphtha, steam cracker naphta or mixtures thereof.
  • the naphtha is straight-run.
  • C6+ heavy naphtha is also preferred.
  • a C6+ heavy naphtha is a heavy naphtha that consists essentially of molecules with 6 or more carbon atoms.
  • the dehydrogenation of the heavy naphtha of step (i) is carried out at typical temperature higher than 250°C, preferably between 250°C and 650°C, more preferably between 350°C and 650°C and more preferably between 480°C and 530 °C.
  • the pressure of the system in this step is typically between 1 and 80 bar, and preferably between 3 and 30 bar.
  • the aromatic compounds are typically produced in the dehydrogenation of heavy naphtha in the presence of at least one reforming catalyst of step (i).
  • the content of naphthenes is typically reduced after the dehydrogenation of heavy naphtha in the presence of at least one reforming catalyst of step (i).
  • excellent results are obtained when the amount of naphthenes is as low as possible and the amount of aromatic compounds is as high as possible.
  • at least a 20% by weight of the stream of naphtha used in step (ii) are aromatics and less than a 1 % by weight of the stream of naphtha used in step (ii) are naphthenes.
  • a reforming catalyst is used in step (i). It will be understood by those having skill in the art that there may be more than one reforming catalyst in step (i). Examples of useful reforming catalysts used in step (i) as herein disclosed include Pt, Re, Ir, Ge, Sn or mixtures thereof supported over alumina.
  • the reforming catalyst could be preferably selected from RG-582 and RG-682 of Axens or R62, R86, R56 and R98 of UOP or mixtures thereof.
  • At least 90% of the hydrogen produced at the stage of dehydrogenation is separated between steps (i) and (ii) or between steps (ii) and (iii).
  • essentially all the hydrogen produced at the stage of dehydrogenation is separated between steps (i) and (ii) or between steps (ii) and (iii). Even more preferably, more than 99 % of the hydrogen produced is separated.
  • an alkylation step (ii) is carried out.
  • the olefins are alkylated with the aromatic compounds produced in step (i) or oligomerised by reacting among them, giving rise to a new hydrocarbon stream, which is rich in compounds with a distillation range of 150+ (products that distillate at temperature above 150°C according to standard ASTM D86).
  • the alkylation of aromatic compounds with olefinic streams, using a solid acid catalyst such as zeolites, acidic resins or supported phosphoric acid, to produce alkylaromatics and oligomers, is studied in the literature.
  • the production of the middle distillate fraction is typically between 10 and 70% weight/weight of the initial mixture of compounds obtained in step (ii).
  • the fraction rich in gasoline is typically between 30 and 90% weight/weight of the initial mixture of compounds obtained in step (ii).
  • the fraction rich in LPG is typically less than 45% of the mixture of compounds obtained in step (ii).
  • octane number sometimes called “octane rating” is a scale that measures the anti-knock capacity of the fuel (such as gasoline) when it is compressed inside an engine cylinder.
  • octane rating is a scale that measures the anti-knock capacity of the fuel (such as gasoline) when it is compressed inside an engine cylinder.
  • Hydrogenation Process whereby a hydrocarbon molecule loses one or more Hydrogen molecules. When it is applied to the production of aromatic compounds, each hydrocarbon molecule loses 3 hydrogen molecules.
  • Alkylation Chemical process whereby an aromatic compound and an olefin react to form an alkyl aromatic compound.
  • gasoline refers to any liquid fuel that can be used to operate a spark ignition internal combustion engine.
  • Gasoline typically contains a mixture of C5 to C10 hydrocarbons having a boiling range of about 70 °C to 160 °C (ASTM D86).
  • MCM catalysts are known in the art, and can be obtained from, for example, ExxonMobil Catalyst Technologies LLC (Baytown, TX). MCM type catalysts, including synthesis details, are described in, for example, the patents U.S. 7198711 , US 5639931 , US 5296428 , US 5146029 and U.S. Application 2006/0194998 . Each of these references are hereby incorporated by reference in their entirety.
  • Acid resin is understood to mean a matrix made of an organic polymer.
  • the structure presents pores wherein ions may be exchanged, which makes them capable of being used in purification and separation.
  • the most typical resins are based on a cross-linked polystyrene matrix, which is obtained by adding another compound, such as, for example, divinylbenzene, to styrene during the polymerisation process.
  • Another compound such as, for example, divinylbenzene
  • protons from the surface thereof By substituting protons from the surface thereof with other organic groups, it is possible to functionalise the resins, such that they may be acidic or basic.
  • acid resins have sulfonic acid groups inside them.
  • resins are CT-275, manufactured by Purolite, or A-15, A-35 and A-36, manufactured by Rohm and Haas. As an application example, they are used industrially for the production of ethers, as described in patents US 4423251 and US 4540831 .
  • Tables 1 and 2 list the typical compositions of the major streams that are obtained throughout the typical process described in Figure 1 .
  • Table 1 Stream (see Fig. 1 ) S, ppm weight N, ppm weight Naphthenes, % by weight Aromatics, % by weight Olefins, % by weight Initial Boiling Point °C Final Boiling Point °C Feed (A) 0.5 0.5 40 15 0 85 180 Output from dehydrogenation section (B) 0.5 0.5 1 52 0 50 180 Stream Rich in aromatics (G) 0.5 0.5 1 84 0 80 180 Stream rich in olefins (H) 10 1 0 0 80 20 50 Output from alkylation (K) ⁇ 10 1 1 60 20 52 342 Table 2 Stream (see fig.

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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)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
EP12382067.2A 2012-02-24 2012-02-24 Procédé de production de distillats moyens Not-in-force EP2631282B1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP12382067.2A EP2631282B1 (fr) 2012-02-24 2012-02-24 Procédé de production de distillats moyens
ES12382067.2T ES2541052T3 (es) 2012-02-24 2012-02-24 Proceso para la producción de destilados medios

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EP2631282B1 EP2631282B1 (fr) 2015-04-08

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020131335A1 (fr) * 2018-12-17 2020-06-25 Saudi Arabian Oil Company Procédé et processus pour maximiser le rendement diesel

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10669490B2 (en) 2016-01-25 2020-06-02 Dupont Industrial Biosciences Usa, Llc Process for producing diesel with low levels of sulfur

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US2295808A (en) * 1940-09-13 1942-09-15 Universal Oil Prod Co Treatment of hydrocarbons
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US4423251A (en) 1982-09-09 1983-12-27 Uop Inc. Process employing sequential isobutylene hydration and etherification
US4431522A (en) 1983-03-09 1984-02-14 Uop Inc. Catalytic reforming process
US4540831A (en) 1984-05-17 1985-09-10 Uop Inc. Mixed-phase hydrocarbon conversion process employing total overhead condenser
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US5639931A (en) 1993-10-18 1997-06-17 Mobil Oil Corporation Process for producing low aromatic diesel fuel with high cetane index
WO2000039253A1 (fr) 1998-12-29 2000-07-06 Mobil Oil Corporation Amelioration de cetane par alkylation aromatique
WO2001083408A1 (fr) 2000-04-28 2001-11-08 Mobil Oil Corporation Regeneration de catalyseurs d'alkylation aromatiques par degazolinage d'hydrocarbure
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US20060194998A1 (en) 2005-02-28 2006-08-31 Umansky Benjamin S Process for making high octane gasoline with reduced benzene content
US20070038007A1 (en) * 2003-03-10 2007-02-15 Ivan Greager Production of linear alkyl benzene
US7198711B1 (en) 2000-01-21 2007-04-03 Exxonmobil Research And Engineering Company Catalytic cracking processing using an MCM-68 catalyst
WO2008043066A2 (fr) 2006-10-05 2008-04-10 Syntroleum Corporation Procédé pour produire un distillat moyen

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US290460A (en) 1883-12-18 Boot or shoe
US791639A (en) 1904-11-26 1905-06-06 Jacob Rosin Miller Saw cotton-gin.
US2295808A (en) * 1940-09-13 1942-09-15 Universal Oil Prod Co Treatment of hydrocarbons
US3019180A (en) * 1959-02-20 1962-01-30 Socony Mobil Oil Co Inc Conversion of high boiling hydrocarbons
CA1080689A (fr) 1971-01-25 1980-07-01 Uop Inc. Procede de conversion d'hydrocarbures et catalyseur utilise a cette fin
US4124491A (en) 1972-05-09 1978-11-07 Uop Inc. Hydrocarbon conversion with a selectively sulfided acidic multimetallic catalytic composite
US4594143A (en) 1982-08-23 1986-06-10 Mobil Oil Corporation Process for reacting light olefins and jet fuel
US4423251A (en) 1982-09-09 1983-12-27 Uop Inc. Process employing sequential isobutylene hydration and etherification
US4431522A (en) 1983-03-09 1984-02-14 Uop Inc. Catalytic reforming process
US4540831A (en) 1984-05-17 1985-09-10 Uop Inc. Mixed-phase hydrocarbon conversion process employing total overhead condenser
US4594144A (en) * 1985-06-14 1986-06-10 Uop Inc. Process for making high octane gasoline
US4740292A (en) 1985-09-12 1988-04-26 Mobil Oil Corporation Catalytic cracking with a mixture of faujasite-type zeolite and zeolite beta
US5146029A (en) 1986-07-29 1992-09-08 Mobil Oil Corporation Olefin interconversion by shape selective catalysis
EP0550120A1 (fr) 1988-03-30 1993-07-07 Uop Catalyseur zéolite bêta activé et procédé d'isomérisation
US4992606A (en) 1988-10-06 1991-02-12 Mobil Oil Corp. Process for preparing short chain alkyl aromatic compounds
US5296428A (en) 1991-01-11 1994-03-22 Mobil Oil Corp. Catalyst comprising MCM-36 and a hydrogenation/dehydrogenation component
US5273644A (en) * 1992-10-13 1993-12-28 Uop Integrated reforming and alkylation process for low benzene reformate
US5380425A (en) * 1993-08-31 1995-01-10 Mobil Oil Corporation Over alkylation and catalytic cracking for benzene conversion
US5639931A (en) 1993-10-18 1997-06-17 Mobil Oil Corporation Process for producing low aromatic diesel fuel with high cetane index
EP0679437A1 (fr) 1994-04-28 1995-11-02 Uop Régénération periodique d'un catalyseur solide d'alkylation avec de l'hydrogène
WO1996020148A1 (fr) 1994-12-27 1996-07-04 Mobil Oil Corporation Processus continu de preparation d'ethylbenzene par alkylation en phase liquide et transalkylation en phase vapeur
US6730625B1 (en) 1998-07-09 2004-05-04 Exxonmobil Oil Corporation Hydroalkylation of aromatic hydrocarbons
WO2000039253A1 (fr) 1998-12-29 2000-07-06 Mobil Oil Corporation Amelioration de cetane par alkylation aromatique
US7198711B1 (en) 2000-01-21 2007-04-03 Exxonmobil Research And Engineering Company Catalytic cracking processing using an MCM-68 catalyst
WO2001083408A1 (fr) 2000-04-28 2001-11-08 Mobil Oil Corporation Regeneration de catalyseurs d'alkylation aromatiques par degazolinage d'hydrocarbure
US20070038007A1 (en) * 2003-03-10 2007-02-15 Ivan Greager Production of linear alkyl benzene
US20060194998A1 (en) 2005-02-28 2006-08-31 Umansky Benjamin S Process for making high octane gasoline with reduced benzene content
WO2008043066A2 (fr) 2006-10-05 2008-04-10 Syntroleum Corporation Procédé pour produire un distillat moyen

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2020131335A1 (fr) * 2018-12-17 2020-06-25 Saudi Arabian Oil Company Procédé et processus pour maximiser le rendement diesel
US11149214B2 (en) 2018-12-17 2021-10-19 Saudi Arabian Oil Company Method and process to maximize diesel yield

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