EP2516597A1 - Procédé de déparaffinage catalytique - Google Patents

Procédé de déparaffinage catalytique

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Publication number
EP2516597A1
EP2516597A1 EP10840062A EP10840062A EP2516597A1 EP 2516597 A1 EP2516597 A1 EP 2516597A1 EP 10840062 A EP10840062 A EP 10840062A EP 10840062 A EP10840062 A EP 10840062A EP 2516597 A1 EP2516597 A1 EP 2516597A1
Authority
EP
European Patent Office
Prior art keywords
catalyst
dewaxing
silica
zsm
less
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.)
Withdrawn
Application number
EP10840062A
Other languages
German (de)
English (en)
Inventor
Christine N. Elia
Timothy Lee Hilbert
Louis Francis Burns
Eric D. Joseck
Jeenok T. Kim
Sylvain S. Hantzer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ExxonMobil Technology and Engineering Co
Original Assignee
ExxonMobil Research and Engineering Co
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 ExxonMobil Research and Engineering Co filed Critical ExxonMobil Research and Engineering Co
Publication of EP2516597A1 publication Critical patent/EP2516597A1/fr
Withdrawn legal-status Critical Current

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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins 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
    • C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax
    • C10G73/02—Recovery of petroleum waxes from hydrocarbon oils; Dewaxing of hydrocarbon oils
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
    • 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
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
    • C10G47/10—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used with catalysts deposited on a carrier
    • C10G47/12—Inorganic carriers
    • 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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV

Definitions

  • the present disclosure relates to a process for catalytically dewaxing feeds having a variety of wax contents.
  • Waxy feedstocks may be used to prepare basestocks having a high viscosity index (VI).
  • VI viscosity index
  • Dewaxing may be accomplished by means of a solvent or catalytically.
  • Solvent dewaxing is a physical process whereby waxes are removed by contacting with a solvent, such as methyl ethyl ketone, followed by chilling to crystallize the wax and filtration to remove the wax.
  • Catalytic dewaxing involves chemically converting the less desirable molecules to produce a basestock with more favorable low temperature properties.
  • Catalytic dewaxing is a process for converting these long chain normal paraffins and slightly branched paraffins to improve the low temperature properties of the feed.
  • Catalytic dewaxing may be accomplished using catalysts that function primarily by cracking waxes to lower boiling products, or by catalysts that primarily isomerize waxes to more highly branched products.
  • Catalysts that dewax by cracking decrease the yield of lubricating oils while increasing the yield of lower boiling distillates.
  • Catalysts that isomerize do not normally result in significant boiling point conversion.
  • Catalysts that dewax primarily by cracking are exemplified by the zeolites ZSM-5, ZSM-1 1, ZSM-12, and offretite.
  • Catalysts that dewax primarily by isomerization are exemplified by the zeolites ZSM-22, ZSM-23, SSZ-32, ZSM-35, and ZSM-48.
  • United States Published Patent Application No. 2007/0131581 discloses ZSM-48 having a silica to alumina molar ratio of 110 or less that is free of non-ZSM-48 seed crystals and free of ZSM-50.
  • the low silica ZSM-48 is shown to have improved activity in the dewaxing of slack wax.
  • the disclosure resides in a catalytic dewaxing process comprising:
  • the catalyst comprises from 50 to 70 wt% of ZSM-48 having a silica to alumina molar ratio of less than 200: 1.
  • the ZSM-48 has a silica to alumina molar ratio of 100: 1 or less.
  • the catalyst comprises from 0.3 to 0.8 wt% of a metal or metal compound from Groups 8 to 10 of the Periodic Table of the Elements, especially platinum.
  • the catalyst further comprises an inorganic oxide binder, such as silica, a silicate, or an aluminosilicate.
  • said dewaxing conditions include a temperature of 365°C or less, such as from 290°C to 365°C, and a liquid hourly space velocity on the hydrocarbon feed of at least 0.4 hr "1 , such as from 0.95 to 3 hr "1 .
  • Figure 1 is a graph comparing the average reaction temperature required to achieve different final pour points with high and low sulfur hydrotreated slack wax feeds using the dewaxing process of Example 3.
  • Figure 2 is a graph comparing the 370°C+ conversion required to achieve different final pour points with high and low sulfur feeds hydrotreated slack wax feeds using the dewaxing process of Example 3.
  • Figure 3 is a graph comparing the average reaction temperature required to achieve different final pour points with different feeds using the dewaxing catalyst of Example 1 and using a similar process but with a higher silica to alumina ZSM-48 catalyst.
  • Figure 4 is a graph comparing the 370°C+ conversion required to achieve different final pour points with different feeds using the dewaxing catalyst of Example 1 and using a similar process but with a higher silica to alumina ZSM-48 catalyst.
  • the term "blocked operation” means that, in dewaxing a first hydrocarbon feedstock having a wax content of less than 50 wt% and a second hydrocarbon feedstock having a wax content of 50 wt% or more, the first feedstock would, for example, be contacted with the catalyst under dewaxing conditions for a certain period of time. The supply of the first feedstock to the reactor would then be terminated or blocked, and the second feedstock would be supplied to the reactor without change-out of the catalyst but normally with the dewaxing conditions being changed to deal with the higher wax content of the feed.
  • the present process employs a dewaxing catalyst comprising from 40 to 80 wt%, such as from 50 to 70 wt%, of ZSM-48 zeolite having a silica to alumina molar ratio of less than 200: 1, typically 100: 1 or less, and from 0.3 to 1.5 wt%, such as from 0.3 to 0.8 wt%, of a hydrogenation metal or metal compound from Groups 8 to 10 of the Periodic Table of the Elements.
  • the metal or metal compound from Groups 8 to 10 is platinum or a compound thereof and is incorporated in the catalyst by impregnation or ion exchange.
  • ZSM-48 is a zeolite having 10-ring unidirectional pores.
  • ZSM-48, its X-ray diffraction pattern and a method for its preparation are described in each of U.S. Patent Nos. 4,375,573, 4,397,827, 4,448,675 and 4,423,021.
  • ZSM-48 has a silica/alumina molar ratio in excess of 200: 1.
  • the low silica/alumina ZSM-48 employed in the present process can be prepared by crystallizing a reaction mixture comprising silica, alumina, base, water and a directing agent (R) comprising a hexamethonium ( ⁇ , ⁇ , ⁇ , ⁇ ', ⁇ ', ⁇ '-hexamethyl- 1 ,6-hexanediammonium) salt, particularly hexamethonium dichloride or dihydroxide.
  • the reaction mixture has the following composition.
  • SiO 2 0.01-0.05, preferably 0.015 to 0.025
  • the crystallization is generally conducted by stirring the reaction mixture at a temperature of 100 to 250°C and produces ZSM-48 crystals having a silica: alumina molar ratio of 70 to 1 10 and a crystal size in the range of 0.01 to 1 ⁇ . More information on this process for producing low silica/alumina ZSM-48 can be found in U.S. Published Patent Application No. 2007/0131581 , the entire contents of which are incorporated herein by reference.
  • the catalyst employed in the present process typically also contains from 20 to 60 wt% of a binder or matrix material. Binders are attrition resistant and resistant to the temperatures experienced by the catalyst in use. Binders may be catalytically active or inactive and include other zeolites, other inorganic materials such as clays and metal oxides, such as alumina, titania, silica and silica-alumina. Clays may be kaolin, bentonite and montmorillonite and are commercially available.
  • suitable porous matrix materials in addition to silica-aluminas include other binary materials such as silica-magnesia, silica-thoria, silica-zirconia, silica- beryllia and silica-titania as well as ternary materials such as silica-alumina- magnesia, silica-alumina-thoria and silica-alumina-zirconia.
  • the present process can be employed in the isomerization dewaxing of a wide variety of lube oil feedstocks.
  • feedstocks are generally wax-containing feeds that boil in the lubricating oil range, typically having a 10% distillation point greater than 650°F (343°C), measured by ASTM D 86 or ASTM D2887.
  • feeds may be derived from a number of sources such as oils derived from solvent refining processes such as raffinates, partially solvent dewaxed oils, deasphalted oils, distillates, hydrocracker bottoms, vacuum gas oils, coker gas oils, slack waxes, foots oils and the like, and Fischer- Tropsch waxes.
  • Slack waxes are typically derived from hydrocarbon feeds by solvent or propane dewaxing. Slack waxes contain some residual oil and are typically deoiled. Foots oils are derived from deoiled slack waxes. Fischer- Tropsch waxes are prepared by the Fischer- Tropsch synthetic process.
  • the feedstocks employed in the present process may have high contents of nitrogen and/or sulfur contaminants.
  • feeds having a nitrogen content of up to 80 ppm, even up to 150 ppm, and/or a sulfur content of up to 250 ppm, even up 1000 ppm can be processed in the present process.
  • Sulfur and nitrogen contents may be measured by standard ASTM methods D2622 and D4629, respectively.
  • Suitable conditions for the present dewaxing process include temperatures of up to 426°C, preferably 365°C or less, more preferably 290°C to 365°C, pressures of from 791 to 20786 kPa (100 to 3000 psig), preferably 1480 to 17339 kPa (200 to 2500 psig), liquid hourly space velocities of from 0.1 to 10 hr "1 , preferably at least 0.4 hr "1 , more preferably from 0.95 to 3 hr "1 , and hydrogen treat gas rates from 45 to 1780 m 3 /m 3 (250 to 10000 scf/B), preferably 89 to 890 m 3 /m 3 (500 to 5000 scf/B).
  • Suitable hydrotreating catalysts contain Group 6 metals, Group 8-10 metals, and mixtures thereof.
  • suitable metals include nickel, tungsten, molybdenum, cobalt and mixtures thereof. These metals are typically present as oxides or sulfides on refractory metal oxide supports.
  • the mixture of metals may also be present as bulk metal catalysts wherein the amount of metal is 30 wt% or greater, based on catalyst.
  • Suitable metal oxide supports include oxides such as silica, alumina, silica-aluminas or titania, preferably alumina.
  • Preferred aluminas are porous aluminas such as gamma or eta.
  • the amount of metal either individually or in mixtures, ranges from 0.5 to 35 wt%, based on the catalyst.
  • Suitable hydrotreating conditions include temperatures of up to 426°C, such as from 150 to 400°C, for example from 200 to 350°C, a hydrogen partial pressure of from 1480 to 20786 kPa (200 to 3000 psig), such as from 2859 to 13891 kPa (400 to 2000 psig), a space velocity of from 0.1 to 10 hr "1 , such as from 0.1 to 5 hr "1 , and a hydrogen to feed ratio of from 89 to 1780 m 3 /m 3 (500 to 10000 scf/B), preferably 178 to 890 m 3 /m 3 .
  • the dewaxing catalyst employed in this Example comprised of 65 wt% of ZSM-48 having a silica to alumina molar ratio of 90/1 and 35 wt% alumina in the form of a 1.5mm diameter by 3.25mm length quadrulobe extrudate. This extrudate was steamed for 3 hours at 482°C prior to impregnation with 0.3 wt% platinum (as tetraammine platinum nitrate salt). The catalyst was loaded into a vertical downflow reactor beneath a top bed of a hydrotreating catalyst comprising 15 wt% Pt/Pd on alumina.
  • Example 2 is a hypothetical example using the dewaxing catalyst and process conditions of Example 1 to process a similar set of feeds but having higher levels of sulfur and nitrogen impurities.
  • the operating temperatures required to achieve the same 370°C+ conversion as in Example 1 were calculated and the results are shown in Table 2.
  • Table 2 shows that, depending on the wax content of the feed, high levels of sulfur and nitrogen that can be tolerated at nominal 365°C dewaxing temperature with the catalyst of Example 1. Note that the conversion levels are the same in Example 2 as Example 1 thus leading to similar lube yields and properties.
  • Example 2 the dewaxing catalyst of Example 1 was used to dewax two similar slack wax feeds that had undergone prior hydrotreatment with a conventional NiMo on alumina HDT catalyst under similar conditions as specified in Table 3 but with the temperature adjusted to result in hydrotreated products with different sulfur levels.
  • a dual catalyst comprising a top bed of a hydrotreating catalyst comprising 15 wt% Pt/Pd on alumina and a bottom bed of a dewaxing catalyst.
  • the dewaxing catalyst comprised 65 wt% of ZSM-48 having a silica to alumina molar ratio of 90/1 and 35 wt% alumina in the form of a 1.5mm diameter by 3.25mm length quadrulobe extrudate.
  • the extrudate was steamed for 3 hours at 482°C prior to impregnation with 0.6 wt% platinum (as tetraammine platinum nitrate salt).
  • the feed was treated at a 421 Nm 3 /m 3 hydrogen circulation rate, an LHSV of 1.33 hr ⁇ l, a pressure of 1600 psig (1 1133 kPa) and at the temperatures shown in Table 4.
  • the results are also shown in Table 4 and demonstrate that the high activity catalyst, by allowing dewaxing to be effected at lower temperatures, permits higher sulfur content feeds to be processed while maintaining reasonable lube yields.
  • Feed A a medium pressure hydrocrackate (MPHC) and Feed B: a lube hydrocrackate (LHDC), were investigated in this Example.
  • the feeds had the properties shown in Table 5.
  • the feeds were dewaxed using two different ZSM-48 catalysts.
  • the first catalyst was the same dewaxing catalyst employed in Example 1.
  • the second catalyst comprised 65 wt% of ZSM-48 having a silica to alumina molar ratio of 200/1 and 35 wt% alumina in the form of a 1.5mm diameter by 3.25mm length quadrulobe extrudate.
  • the extrudate was steamed for 3 hours at 482°C prior to impregnation with 0.6 wt% platinum (as tetraammine platinum nitrate salt).
  • the feed was treated at a 421 NmVm 3 hydrogen circulation rate, an LHSV of 1.33 hr "1 , a pressure of 2000 psig (13789 kPa).
  • the results are shown in Figures 3 and 4 and demonstrate that the low silica/alumina ratio catalyst of Example 1 at a Pt content of only 0.3 wt% exhibits similar activity and selectivity (as measured by 370°C+ conversion) to the higher silica/alumina ratio catalyst with a Pt content of 0.6 wt%.
  • This example teaches that the higher zeolite activity can be compensated for by lowering the metal content.
  • Feed B used in Example 5 is similar to the feed used in Example 4. Processing conditions are also similar between the two examples, although there is a 400 psig difference in pressure. If one compares the no sulfur result in Example 4 which used a catalyst comprised of 90/1 Si/A12 crystal and 0.6 wt% Pt to the Feed B result processed with 0.3 wt% Pt and 90/1 Si/Al 2 ratio, one can see that increasing the metal content from 0.3 wt% to 0.6 wt% increases the catalyst activity.
  • Example 4 required only 329°C to achieve a -25 °C pour point, while the catalyst from Example 5 with half the metal required approximately 340°C to achieve a similar pour point.

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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)
  • Inorganic Chemistry (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé de déparaffinage catalytique, selon lequel un catalyseur comprenant de 40 à 80 % en poids de ZSM-48 ayant un rapport molaire de la silice sur l'alumine inférieur à 200/1 et 0,3 à 1,5 % en poids d'un métal ou d'un composé métallique des groupes 8 à 10 de la classification périodique des éléments étant placé dans une zone de réaction. Le catalyseur est périodiquement mis en contact dans la zone de réaction, dans des conditions de déparaffinage, avec une première charge d'hydrocarbure ayant une teneur en cire inférieure à 50 % en poids et une seconde charge d'hydrocarbure ayant une teneur en cire de 50 % en poids ou plus.
EP10840062A 2009-12-24 2010-12-21 Procédé de déparaffinage catalytique Withdrawn EP2516597A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US28483509P 2009-12-24 2009-12-24
PCT/US2010/061542 WO2011079116A1 (fr) 2009-12-24 2010-12-21 Procédé de déparaffinage catalytique

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EP2516597A1 true EP2516597A1 (fr) 2012-10-31

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US (1) US20110180453A1 (fr)
EP (1) EP2516597A1 (fr)
JP (1) JP2013515821A (fr)
KR (1) KR20120114321A (fr)
CN (1) CN102686709A (fr)
CA (1) CA2784146A1 (fr)
IN (1) IN2012DN05208A (fr)
RU (1) RU2012128049A (fr)
SG (1) SG181451A1 (fr)
WO (1) WO2011079116A1 (fr)

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EP3397724B1 (fr) 2015-12-28 2024-04-17 ExxonMobil Technology and Engineering Company Procédé de déparaffinage par catalyseur de déparaffinage ayant une activité de saturation d'aromatiques améliorée
EP3397382A1 (fr) 2015-12-28 2018-11-07 ExxonMobil Research and Engineering Company Imprégnation séquentielle d'un support poreux afin de former un alliage de métaux nobles
WO2023015168A1 (fr) 2021-08-06 2023-02-09 ExxonMobil Technology and Engineering Company Procédé d'hydro-désalkylation destiné à générer des carburants de haute qualité, des huiles de base et des cires

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Publication number Publication date
CA2784146A1 (fr) 2011-06-30
KR20120114321A (ko) 2012-10-16
US20110180453A1 (en) 2011-07-28
JP2013515821A (ja) 2013-05-09
CN102686709A (zh) 2012-09-19
WO2011079116A1 (fr) 2011-06-30
RU2012128049A (ru) 2014-01-27
SG181451A1 (en) 2012-07-30
IN2012DN05208A (fr) 2015-10-23

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