US3894938A - Catalytic dewaxing of gas oils - Google Patents

Catalytic dewaxing of gas oils Download PDF

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Publication number
US3894938A
US3894938A US370265A US37026573A US3894938A US 3894938 A US3894938 A US 3894938A US 370265 A US370265 A US 370265A US 37026573 A US37026573 A US 37026573A US 3894938 A US3894938 A US 3894938A
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pour point
sulfur
zeolite
gas oil
dewaxing
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US370265A
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Robert L Gorring
George F Shipman
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ExxonMobil Oil Corp
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Mobil Oil Corp
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Application filed by Mobil Oil Corp filed Critical Mobil Oil Corp
Priority to US370265A priority Critical patent/US3894938A/en
Priority to CA195,627A priority patent/CA1024091A/en
Priority to GB1546674A priority patent/GB1443877A/en
Priority to JP49041825A priority patent/JPS5911635B2/en
Priority to FR7413675A priority patent/FR2233384B1/fr
Priority to ZA00742111A priority patent/ZA742111B/en
Priority to AU69296/74A priority patent/AU484959B2/en
Priority to TR17826A priority patent/TR17826A/en
Priority to BE145340A priority patent/BE816234A/en
Priority to DE19742428463 priority patent/DE2428463A1/en
Priority to NL7407870A priority patent/NL7407870A/xx
Priority to IT23998/74A priority patent/IT1015078B/en
Application granted granted Critical
Publication of US3894938A publication Critical patent/US3894938A/en
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    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/06—Gasoil

Definitions

  • a ZSM-S type zeolite hyd'rodewaxing catalyst which may contain a hydrogenation/dehydrogenation component, in the presence or absence of added hydrogen under low pressure conditions, followed by conventional hydrodesulfurization processing of the dewaxed intermediate.
  • Liquid hydrocarbons in the 400 to 850F boiling range include kerosine, Diesel fuel and No. 2, or home heating fuel. Petroleum fractions boiling in this range often have a significant long chain paraffin content which accounts for their rather high pour point. lt is not unusual for fractions of this type to have pour points in the 50 to lOF range.
  • One significant specification for some No. 2 fuel oil is a pour point of 0F or lower. Thus reduction in pour point is accomplished by dewaxing or removing the long chain normal paraffins which seem to be principally responsible for this property.
  • This dewaxing has traditionally been accomplished by a solvent dewaxing technique according to which the gas oil is thoroughly mixed with a suitable solvent, often methyl ethyl ketone, into which the wax dissolves. ln the past, the wax was recovered from the solvent, by evaporation of the ketone, purified and sold for seals, candles and other uses. More recently, the petroleum industry has seen a marked decline in this market and has therefore sought more profitable and less costly outlets for this wax constituent.
  • shape selective zeolitic catalysts to crack, preferably hydroerack, these paraffinic components and convert them into smaller, suitably paraffinic fragments which may be collected as light gas, or larger but not waxy paraffinic materials which remain in the boiling range of the gas oil being treated and therefore enhance the yield of the dewaxing operation.
  • the smaller cracked fragments may be used as fuel, sold as such or resolved and disposed of by components.
  • ZSM-S type of zeolite is a group of small pored zeoiites, the most noteworthy members of which are ZSM- 5, ZSM-8 and ZSM-l 1.
  • US. Pat. Nos. 3,702,886 directed to ZSlVl-S zeolite and 3,709,979 directed to ZSM-l l zeolite are in point and are incorporated herein by reference.
  • Abandoned US. Patent application Ser. No. 865,418, filed Oct. 10, I969 is directed to ZSM-S and is also in point and is incorporated herein by reference.
  • the ZSM-S family of zeolites can be used to catalyze cracking of normal or slightly branched paraffins in the absence of added hydrogen or to catalyze hydroeracking of such paraffins in the presence of added hydrogen.
  • Typical cracking conditions include a space velocity of about 0.25 to 200 LHSV, a temperature of about 400F to l 100F and a pressure from subatmospheric to several hundred atmospheres.
  • Typical hydrocracking conditions include a space velocity of about 0.1 to 10 LHSV, a hydrogen to hydrocarbon mole ratio of about 1 to to l, a temperature of about 650F to 1000F and a pressure of about l00 to 3000 psig (see US Patent 3,700,585).
  • catalytic hydrodesulfurization is a unit process whichis widely used in a refinery. lt precedes reforming and other conversion processes because sulfur, nitrogen and/or metals present in the charge stock often have detrimental effects upon hydrocarbon conversion catalysts. Metals, sulfur and nitrogen tend to concentrate in the heavier petroleum fractions. Therefore conversion processes utilizing such heavier petroleum fractions would normally be considered prime users of the conventional desulfurization followed by catalytic conversion processing sequenee.
  • one important aspect of this invention resides in a processing sequence consisting essentially of catalytically dewaxing a sulfur and/or nitrogen containing gas oil having a boiling range in the range of about 400F to 900F and thence subjecting at least the liquid product resulting from such dewaxing to desulfurization and/or denitrogenation.
  • the gas oils to which this process is directed have a total sulfur and nitrogen content of at least 0.1 wt. percent and 10 ppm, respectively, and a pour point of at least +20F.
  • a ZSM-S type of zeolite catalyst for dewaxing and to operate the dewaxing portion of this process at about 300 to l000F, 0 to 2000 psig, 0.1 to 10 LHSV and a hydrogen to hydrocarbon ratio of about 0 to 25 to 1.
  • the ZSM-S type zeolite may have incorporated therein a hydrogen transfer functional component such as nickel, palladium, or platinum in a proportion of about 0.5 to 5 weight percent based on the total weight of dewaxing catalyst.
  • the dewaxing catalyst may be used in a fixed or fluidized bed configuration as desired.
  • the catalyst particles In a fixed bed operation, the catalyst particles should be sized be tween one thirty-second and one-eighth inch. in a fluidized bed the catalyst particles should be about 80 to 400 mesh.
  • the catalyst may be of the matrix type with alumina, silica, silica-alumina or other similar known matrix materials. In this matrix embodiment. the ZSM- type'zeolite should constitute about 5 to 95 weight percent of the total catalyst matrix.
  • the product of catalytic dewaxing may be resolved into a liquid and gas portion by cooling to a prescribed temperature at an appropriate pressure to obtain what ever liquid-gas demarcation is desired.
  • the liquid may then be subjected to desulfurization and denitrogenation. It is preferred however to subject the entire de waxed product, without intermediate product resolution, to desulfurization and denitrogenation. By not resolving the intermediate product there is obtained a great saving in energy, particularly heat, because this resolution requires cooling and the subsequent desulfurization and denitrogenation requires reheating.
  • Desulfurization and denitrogenation are usually accomplished simultaneously, one treatment serving to liberate both sulfur and nitrogen from the feed stock. This treatment can be carried out in any manner desired, e.g.
  • EXAMPLE 1 (PRIOR ART) A gas oil having a boiling range of 500 to 800F, a
  • EXAMPLE 2 (PRIOR ART) A gas oil having a boiling range of 500 to 800F, a pour point of +50F, a sulfur content of 2.5 percent and a nitrogen content of 0.02 percent was contacted with a cobalt-molybdenum-alumina catalyst at 700F, 400 psig, 5.0 hydrogen to hydrocarbon ratio and 1.0 LHSV. The product thus formed was directly, and without intermediate product resolution. contacted with ZSM-5 zeolite at 700F. 400 psig. 50 hydrogen to hydrocarbon mole ratio and 3.0 LHSV. The yield of 330F liquid was 96 percent. However. its pour point was reduced only from +50F to +25F, indicating that the ZSM-S dewaxing catalyst was substantially deactivated.
  • Example 2 was exactly repeated except that the sequence of processing steps was reversed. The yield of 330F+ liquid was 84 percent and the pour point was reduced from +50F to 0F. Time between ZSM-5 catalyst regenerations was 20 days.

Abstract

Improved catalytic dewaxing and desulfurization of high pour point, high sulfur gas oils to lower their pour point to about 10*F or lower and their sulfur content by contacting a high pour point gas oil first with a ZSM-5 type zeolite hydrodewaxing catalyst which may contain a hydrogenation/dehydrogenation component, in the presence or absence of added hydrogen under low pressure conditions, followed by conventional hydrodesulfurization processing of the dewaxed intermediate.

Description

United States Patent [1 1 Gorring et al.
[ 1 July 15, 1975 CATALYTIC DEWAXING OF GAS OILS [73] Assignee: Mobil Oil Corporation, New York,
[22] Filed: June 15, 1973 [21] App]. N0.: 370,265
[52] US. Cl.
[51] Int. Cl. C10G 37/00 [58] Field of Search 208/97, 46
[56] References Cited UNITED STATES PATENTS 3,438,887 4/1969 Morris et a1. 208/97 3,472,759 10/1969 Masolocites et a1. 208/97 3,516,925 6/1970 Lawrence et a1. v 208/46 3668113 6/1972 Burbidge et a1. 208/97 3,700,585 10/1972 Chen et a1. 208/111 3,764,516 10/1973 Steinmetz et a1. 208/97 FOREIGN PATENTS OR APPLICATIONS 884,752 12/1961 United Kingdom 208/97 1,191,471 5/1970 United Kingdom 208/97 Primary Examiner'-De1bert E. Gantz Assistant Examiner' lames W. l-lellwege Attorney, Agent, or FirmCharles A. l-luggett; Michael G. Gilman ABSTRACT Improved catalytic dewaxing and desulfurization of high pour point, high sulfur gas oils to lower their pour point to.about 10F or lower and their sulfur content by contacting a high pour point gas oil first with a ZSM-S type zeolite hyd'rodewaxing catalyst which may contain a hydrogenation/dehydrogenation component, in the presence or absence of added hydrogen under low pressure conditions, followed by conventional hydrodesulfurization processing of the dewaxed intermediate.
4 Claims, N0 Drawings 1 CATALYTTC DEWAXING OF GAS OILS This invention relates to petroleum processing. It more particularly refers to upgrading certain gas oil fractions to low pour point fuels.
Liquid hydrocarbons in the 400 to 850F boiling range include kerosine, Diesel fuel and No. 2, or home heating fuel. Petroleum fractions boiling in this range often have a significant long chain paraffin content which accounts for their rather high pour point. lt is not unusual for fractions of this type to have pour points in the 50 to lOF range. One significant specification for some No. 2 fuel oil is a pour point of 0F or lower. Thus reduction in pour point is accomplished by dewaxing or removing the long chain normal paraffins which seem to be principally responsible for this property.
This dewaxing has traditionally been accomplished by a solvent dewaxing technique according to which the gas oil is thoroughly mixed with a suitable solvent, often methyl ethyl ketone, into which the wax dissolves. ln the past, the wax was recovered from the solvent, by evaporation of the ketone, purified and sold for seals, candles and other uses. More recently, the petroleum industry has seen a marked decline in this market and has therefore sought more profitable and less costly outlets for this wax constituent.
It has therefore been proposed to use shape selective zeolitic catalysts to crack, preferably hydroerack, these paraffinic components and convert them into smaller, suitably paraffinic fragments which may be collected as light gas, or larger but not waxy paraffinic materials which remain in the boiling range of the gas oil being treated and therefore enhance the yield of the dewaxing operation. The smaller cracked fragments may be used as fuel, sold as such or resolved and disposed of by components.
Most recently it has been proposed to utilize the new ZSM-S type of zeolite as a cracking or hydrocracking dewaxing catalyst because it converts not only the normal paraffins but the slightly branched paraffins as well thereby more efficiently lowering the pour point of the product with better yields than have heretofore been achieved. (See US. Pat. No. 3,700,585).
ZSM-S type of zeolite is a group of small pored zeoiites, the most noteworthy members of which are ZSM- 5, ZSM-8 and ZSM-l 1. US. Pat. Nos. 3,702,886 directed to ZSlVl-S zeolite and 3,709,979 directed to ZSM-l l zeolite are in point and are incorporated herein by reference. Abandoned US. Patent application Ser. No. 865,418, filed Oct. 10, I969 is directed to ZSM-S and is also in point and is incorporated herein by reference. The ZSM-S family of zeolites can be used to catalyze cracking of normal or slightly branched paraffins in the absence of added hydrogen or to catalyze hydroeracking of such paraffins in the presence of added hydrogen. Typical cracking conditions include a space velocity of about 0.25 to 200 LHSV, a temperature of about 400F to l 100F and a pressure from subatmospheric to several hundred atmospheres. Typical hydrocracking conditions include a space velocity of about 0.1 to 10 LHSV, a hydrogen to hydrocarbon mole ratio of about 1 to to l, a temperature of about 650F to 1000F and a pressure of about l00 to 3000 psig (see US Patent 3,700,585).
For most petroleum processing, it is conventional to pretreat the charge stock in some manner calculated to remove sulfur and/or metals and/or nitrogen from the charge stock prior to converting and upgrading such charge stock. Thus catalytic hydrodesulfurization is a unit process whichis widely used in a refinery. lt precedes reforming and other conversion processes because sulfur, nitrogen and/or metals present in the charge stock often have detrimental effects upon hydrocarbon conversion catalysts. Metals, sulfur and nitrogen tend to concentrate in the heavier petroleum fractions. Therefore conversion processes utilizing such heavier petroleum fractions would normally be considered prime users of the conventional desulfurization followed by catalytic conversion processing sequenee.
Thus in the dewaxing of sulfur containing gas oils boiling in the 400 to 900F range, or any part thereof, one of ordinary skill in the art would conventionally think of subjecting such gas oils to catalytic hydrodesulfurization prior to dewaxing. Indeed this may be a desirable modus operandi for dewaxing of gas oils with a conventional shape selective catalyst of the erionite type. It has been most unexpectedly found however that operating according to this sequence with ZSM-S type zeolite dewaxing catalyst leads to a significantly decreased activity as compared to what one would expect (see Examples l and 2 infra). In fact the evidence would seem to lead one to the conclusion that the more sulfur and/or nitrogen there is in the gas oil charge stock, the greater is the diminution of ZSM-5 type zeolite catalyst life. Yet the product finally produced as a result of this dewaxing operation must have a reduced sulfur and/or nitrogen content or preferably substantially no sulfur or nitrogen content at all. This is because this product goes predominantly into the jet fuel, Diesel fuel and home heating market, where nitrogen and sulfur emissions must be closely controlled.
It is therefore an important object of this invention to provide an efficient gas oil dewaxing, desulfurization and denitrogenation process.
It is another object of this invention to provide such a process capable of taking advantage of the use of ZSM-5 type of zeolite dewaxing catalyst.
It is a further object of this invention to provide such a process for producing high yields of No. 2 fuel oil having a pour point of about 0F.
Other and additional objects of this invention will become apparent from a consideration of this entire specification including the claims hereof.
In accord with and fulfilling these objects, one important aspect of this invention resides in a processing sequence consisting essentially of catalytically dewaxing a sulfur and/or nitrogen containing gas oil having a boiling range in the range of about 400F to 900F and thence subjecting at least the liquid product resulting from such dewaxing to desulfurization and/or denitrogenation. In a preferred aspect of this invention the gas oils to which this process is directed have a total sulfur and nitrogen content of at least 0.1 wt. percent and 10 ppm, respectively, and a pour point of at least +20F. It is preferred to use a ZSM-S type of zeolite catalyst for dewaxing and to operate the dewaxing portion of this process at about 300 to l000F, 0 to 2000 psig, 0.1 to 10 LHSV and a hydrogen to hydrocarbon ratio of about 0 to 25 to 1. Where the dewaxing portion of the process is of the hydrodewaxing type, the ZSM-S type zeolite may have incorporated therein a hydrogen transfer functional component such as nickel, palladium, or platinum in a proportion of about 0.5 to 5 weight percent based on the total weight of dewaxing catalyst. The dewaxing catalyst may be used in a fixed or fluidized bed configuration as desired. In a fixed bed operation, the catalyst particles should be sized be tween one thirty-second and one-eighth inch. in a fluidized bed the catalyst particles should be about 80 to 400 mesh. The catalyst may be of the matrix type with alumina, silica, silica-alumina or other similar known matrix materials. In this matrix embodiment. the ZSM- type'zeolite should constitute about 5 to 95 weight percent of the total catalyst matrix.
' The product of catalytic dewaxing may be resolved into a liquid and gas portion by cooling to a prescribed temperature at an appropriate pressure to obtain what ever liquid-gas demarcation is desired. The liquid may then be subjected to desulfurization and denitrogenation. It is preferred however to subject the entire de waxed product, without intermediate product resolution, to desulfurization and denitrogenation. By not resolving the intermediate product there is obtained a great saving in energy, particularly heat, because this resolution requires cooling and the subsequent desulfurization and denitrogenation requires reheating. Desulfurization and denitrogenation are usually accomplished simultaneously, one treatment serving to liberate both sulfur and nitrogen from the feed stock. This treatment can be carried out in any manner desired, e.g. conventionally at about 550 to 800F, 200 to l000 psig, 0.5 to 4.0 LHSV. 2 to moles of added hydrogen per mole of feed stock, in effective contact with a cobalt-molybdenum-alumina-catalyst. This procedure converts sulfur and nitrogen values in the feed stock to hydrogen sulfide and ammonia which are later recovered from the gaseous portion of the final product.
While operating in the manner and sequence set forth results in excellent dewaxing and pour point reduction to acceptable levels with liquid yields of over about 80 percent and dewaxing catalyst life of about to 400 days between regenerations to a total life of about 6 to 60 months, reversing the sequence of operations, that is desulfurizing and denitrogenating under the same conditions as set forth above and directly dewaxing the intermediate product thus formed to the same final product specifications. permitted operation of the dewaxing catalyst for about 1 to 24 hours between regenerations.
This invention will be illustrated by the following Examples which are not to be considered as limiting on the scope or applicability thereof. In these Examples parts and percentages are by weight unless expressly stated to be on some other basis.
EXAMPLE 1 (PRIOR ART) A gas oil having a boiling range of 500 to 800F, a
pour point of +50F, a sulfur content of less than 3 wt. 7( and a nitrogen content of less than 3000 ppm was contacted with ZSM5 zeolite at 700F. 400 psig. 5.0 hydrogen to hydrocarbon mole ratio and 3.0 LHSV. The conversion to 330F liquid was 84 percent with the pourpoint reduced to 0F. Time between catalyst regenerations was 20 days.
EXAMPLE 2 (PRIOR ART) A gas oil having a boiling range of 500 to 800F, a pour point of +50F, a sulfur content of 2.5 percent and a nitrogen content of 0.02 percent was contacted with a cobalt-molybdenum-alumina catalyst at 700F, 400 psig, 5.0 hydrogen to hydrocarbon ratio and 1.0 LHSV. The product thus formed was directly, and without intermediate product resolution. contacted with ZSM-5 zeolite at 700F. 400 psig. 50 hydrogen to hydrocarbon mole ratio and 3.0 LHSV. The yield of 330F liquid was 96 percent. However. its pour point was reduced only from +50F to +25F, indicating that the ZSM-S dewaxing catalyst was substantially deactivated.
EXAMPLE 3 Example 2 was exactly repeated except that the sequence of processing steps was reversed. The yield of 330F+ liquid was 84 percent and the pour point was reduced from +50F to 0F. Time between ZSM-5 catalyst regenerations was 20 days.
What is claimed is:
1. In the process of reducing the pour point of a sulfur and nitrogen containing gas oil boiling in the range of 400 to 900F by treating such with a ZSM-S type of zeolite at about 300 to I000F; the improvement, whereby reducing the pour point of said gas oil and purifying such to reduce the sulfur and nitrogen content thereof, which comprises subjecting said gas oil first to said zeolite treatment and then subjecting the whole, unresolved zeolite treated, reduced pour point intermediate to desulfurization and denitrogenation.
2. The improved process claimed in claim 1 wherein said hydrodesulfurization is carried out at about 550 to 800F, 200 to l000 psig hydrogen partial pressure, 0.5 to 4.0 LHSV and in effective contact with a cobaltmolybdenum-alumina catalyst.
3. The improved process claimed in claim 1 wherein said gas oil has a minimum of 0.1 wt. percent total sulfur and 10 ppm nitrogen before processing.
4. The improved process claimed in claim 1 wherein said zeolite treating is carried out at a hydrogen partial pressure of about 0 to 2000 psig and a space velocity of about 0.1 to 10 LHSV.

Claims (4)

1. IN THE PROCESS OF REDUCING THE POUR POINT OF A SULFUR AND NITROGEN CONTAINING GAS OIL BOILING IN THE RANGE OF 400* TO 900*F BY TREATING SUCH WITH A ZSM-5 TYPE OF ZEOLITE AT ABOUT 300* TO 1000*F. THE IMPROVEMENT, WHEREBY REDUCING THE POUR POINT OF SAID GAS OIL AND PURIFYING SUCH TO REDUCE THE SULFUR AND NITROGEN CONTENT THEREOF, WHICH COMPRISES SUBJECTING SAID GAS OIL FIRST TO SAID ZEOLITE TREATMENT AND THEN SUBJECTING THE WHOLE, UNRESOLVED ZEOLITE TREATED, REDUCED POUR POINT INTERMEDIATE TO DESULFURIZATION AND DENITROGENATION.
2. The improved process claimed in claim 1 wherein said hydrodesulfurization is carried out at about 550* to 800* F, 200 to 1000 psig hydrogen partial pressure, 0.5 to 4.0 LHSV and in effective contact with a cobaltmolybdenum-alumina catalyst.
3. The improved process claimed in claim 1 wherein said gas oil has a minimum of 0.1 wt. percent total sulfur and 10 ppm nitrogen before processing.
4. The improved process claimed in claim 1 wherein said zeolite treating is carried out at a hydrogen partial pressure of about 0 to 2000 psig and a space velocity of about 0.1 to 10 LHSV.
US370265A 1973-06-15 1973-06-15 Catalytic dewaxing of gas oils Expired - Lifetime US3894938A (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
US370265A US3894938A (en) 1973-06-15 1973-06-15 Catalytic dewaxing of gas oils
CA195,627A CA1024091A (en) 1973-06-15 1974-03-21 Catalytic dewaxing of gas oils
GB1546674A GB1443877A (en) 1973-06-15 1974-04-08 Catalytic dewaxing of gas oils
JP49041825A JPS5911635B2 (en) 1973-06-15 1974-04-16 Catalytic dewaxing method for gas oil
FR7413675A FR2233384B1 (en) 1973-06-15 1974-04-19
ZA00742111A ZA742111B (en) 1973-06-15 1974-04-22 Catalytic dewaxing of gas oils
AU69296/74A AU484959B2 (en) 1973-06-15 1974-05-23 Catalytic dewaxing of gas oils
TR17826A TR17826A (en) 1973-06-15 1974-06-04 CLEANING GAS-OLS FROM CANDLE CATALYTIC
BE145340A BE816234A (en) 1973-06-15 1974-06-12 CATALYTIC DEPARAFFINING OF GAS-OILS
DE19742428463 DE2428463A1 (en) 1973-06-15 1974-06-12 PROCESS FOR DESULFURIZATION AND DENITROGENATION OF GAS OIL
NL7407870A NL7407870A (en) 1973-06-15 1974-06-12
IT23998/74A IT1015078B (en) 1973-06-15 1974-06-14 PROCEDURE OF DESULPHURATION AND DENITRURING OF HIGH BOILING POINT GASOLS

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JP (1) JPS5911635B2 (en)
BE (1) BE816234A (en)
CA (1) CA1024091A (en)
DE (1) DE2428463A1 (en)
FR (1) FR2233384B1 (en)
GB (1) GB1443877A (en)
IT (1) IT1015078B (en)
NL (1) NL7407870A (en)
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US3980550A (en) * 1975-01-09 1976-09-14 Mobil Oil Corporation Catalytic hydrodewaxing
US4137148A (en) * 1977-07-20 1979-01-30 Mobil Oil Corporation Manufacture of specialty oils
DE2854258A1 (en) * 1977-12-20 1979-06-21 Mobil Oil Corp METHOD FOR THE PRODUCTION OF HIGH QUALITY LUBRICANT BASE OIL
US4171257A (en) * 1978-10-23 1979-10-16 Chevron Research Company Petroleum distillate upgrading process
US4176050A (en) * 1978-12-04 1979-11-27 Mobil Oil Corporation Production of high V.I. lubricating oil stock
US4181598A (en) * 1977-07-20 1980-01-01 Mobil Oil Corporation Manufacture of lube base stock oil
DE2929412A1 (en) * 1978-10-23 1980-04-30 Chevron Res METHOD FOR IMPROVING A PETROLEUM DISTILLATE
DE3010094A1 (en) * 1979-03-19 1980-10-02 Chevron Res HYDROCARBON CONVERSION CATALYST
EP0027380A1 (en) * 1979-10-15 1981-04-22 Mobil Oil Corporation A method of preparing a metal-containing zeolite catalyst and the use of the catalyst in dewaxing gas oil
US4292166A (en) * 1980-07-07 1981-09-29 Mobil Oil Corporation Catalytic process for manufacture of lubricating oils
US4313817A (en) * 1979-03-19 1982-02-02 Chevron Research Company Hydrocarbon conversion catalyst and process using said catalyst
US4332670A (en) * 1981-01-14 1982-06-01 Mobil Oil Corporation Catalytic dewaxing of middle distillates
US4357232A (en) * 1981-01-15 1982-11-02 Mobil Oil Corporation Method for enhancing catalytic activity
US4358363A (en) * 1981-01-15 1982-11-09 Mobil Oil Corporation Method for enhancing catalytic activity
US4358362A (en) * 1981-01-15 1982-11-09 Mobil Oil Corporation Method for enhancing catalytic activity
US4400265A (en) * 1982-04-01 1983-08-23 Mobil Oil Corporation Cascade catalytic dewaxing/hydrodewaxing process
US4419220A (en) * 1982-05-18 1983-12-06 Mobil Oil Corporation Catalytic dewaxing process
US4428862A (en) 1980-07-28 1984-01-31 Union Oil Company Of California Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons
US4436614A (en) 1982-10-08 1984-03-13 Chevron Research Company Process for dewaxing and desulfurizing oils
US4437976A (en) 1981-08-07 1984-03-20 Mobil Oil Corporation Two-stage hydrocarbon dewaxing hydrotreating process
US4437975A (en) 1977-07-20 1984-03-20 Mobil Oil Corporation Manufacture of lube base stock oil
US4440630A (en) * 1982-02-08 1984-04-03 Mobil Oil Corporation Process for simultaneous hydrodesulfurization and hydrodewaxing with a catalyst of controlled pore size and metals content
US4458024A (en) * 1982-02-08 1984-07-03 Mobil Oil Corporation Process for hydrotreating petroleum residua and catalyst therefor
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US5391286A (en) * 1993-11-03 1995-02-21 Texaco Inc. Process for catalytic dewaxing of hydrocarbon feedstocks
US5614079A (en) * 1993-02-25 1997-03-25 Mobil Oil Corporation Catalytic dewaxing over silica bound molecular sieve
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US4743355A (en) * 1979-10-15 1988-05-10 Union Oil Company Of California Process for producing a high quality lube oil stock
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US4600497A (en) * 1981-05-08 1986-07-15 Union Oil Company Of California Process for treating waxy shale oils
US4790927A (en) * 1981-05-26 1988-12-13 Union Oil Company Of California Process for simultaneous hydrotreating and hydrodewaxing of hydrocarbons
US4877762A (en) * 1981-05-26 1989-10-31 Union Oil Company Of California Catalyst for simultaneous hydrotreating and hydrodewaxing of hydrocarbons
US4490242A (en) * 1981-08-07 1984-12-25 Mobil Oil Corporation Two-stage hydrocarbon dewaxing hydrotreating process
US4437976A (en) 1981-08-07 1984-03-20 Mobil Oil Corporation Two-stage hydrocarbon dewaxing hydrotreating process
US4440630A (en) * 1982-02-08 1984-04-03 Mobil Oil Corporation Process for simultaneous hydrodesulfurization and hydrodewaxing with a catalyst of controlled pore size and metals content
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EP0091252A1 (en) * 1982-04-01 1983-10-12 Mobil Oil Corporation Two-step catalytic hydrodewaxing-hydrodesulfurization process
US4400265A (en) * 1982-04-01 1983-08-23 Mobil Oil Corporation Cascade catalytic dewaxing/hydrodewaxing process
US4419220A (en) * 1982-05-18 1983-12-06 Mobil Oil Corporation Catalytic dewaxing process
US4664775A (en) * 1982-07-31 1987-05-12 Toa Nenryo Kogyo Kabushiki Kaisha Method for manufacturing low pour point petroleum product with zeolite TSZ
US4436614A (en) 1982-10-08 1984-03-13 Chevron Research Company Process for dewaxing and desulfurizing oils
US4610778A (en) * 1983-04-01 1986-09-09 Mobil Oil Corporation Two-stage hydrocarbon dewaxing process
US4564440A (en) * 1983-07-11 1986-01-14 Mobil Oil Corporation Viscosity index improvement in dewaxed lube basestock by partial desulfurization in hydrotreat bed
US4549955A (en) * 1983-12-05 1985-10-29 Mobil Oil Corporation Process for stabilizing hydroprocessed lubricating oil stocks by the addition of hydrogen sulfide
US4601993A (en) * 1984-05-25 1986-07-22 Mobil Oil Corporation Catalyst composition dewaxing of lubricating oils
US4696732A (en) * 1984-10-29 1987-09-29 Mobil Oil Corporation Simultaneous hydrotreating and dewaxing of petroleum feedstocks
EP0180354A1 (en) * 1984-10-29 1986-05-07 Mobil Oil Corporation Process for hydrotreating and dewaxing petroleum feedstocks
US4568655A (en) * 1984-10-29 1986-02-04 Mobil Oil Corporation Catalyst composition comprising Zeolite Beta
US4767522A (en) * 1984-11-28 1988-08-30 Mobil Oil Corporation Distillate dewaxing process with mixed zeolites
US4960504A (en) * 1984-12-18 1990-10-02 Uop Dewaxing catalysts and processes employing silicoaluminophosphate molecular sieves
US4599162A (en) * 1984-12-21 1986-07-08 Mobil Oil Corporation Cascade hydrodewaxing process
US4919788A (en) * 1984-12-21 1990-04-24 Mobil Oil Corporation Lubricant production process
US4952303A (en) * 1985-07-10 1990-08-28 Mobil Oil Corp. Process for preparing a very high quality lube base stock oil
US4740292A (en) * 1985-09-12 1988-04-26 Mobil Oil Corporation Catalytic cracking with a mixture of faujasite-type zeolite and zeolite beta
US4711710A (en) * 1985-09-23 1987-12-08 Mobil Oil Corporation Process for making improved lubricating oils from heavy feedstock
US4795546A (en) * 1985-09-30 1989-01-03 Chevron Research Company Process for stabilizing lube base stocks derived from neutral oils
US4913797A (en) * 1985-11-21 1990-04-03 Mobil Oil Corporation Catalyst hydrotreating and dewaxing process
US4700562A (en) * 1986-01-08 1987-10-20 Mobil Oil Corporation Method for determining effectiveness of catalytic dewaxing reactor
US4846959A (en) * 1987-08-18 1989-07-11 Mobil Oil Corporation Manufacture of premium fuels
US4869806A (en) * 1987-12-09 1989-09-26 Mobil Oil Corp. Production of high viscosity index lubricating oil stock
US4853103A (en) * 1988-04-11 1989-08-01 Mobil Oil Corporation Lube catalytic dewaxing-hydrotreating process
US4986894A (en) * 1988-10-06 1991-01-22 Mobil Oil Corp. Catalytic hydroisomerization process
US4994168A (en) * 1988-10-21 1991-02-19 Mobil Oil Corporation Lube oil product stripping
US5015361A (en) * 1989-01-23 1991-05-14 Mobil Oil Corp. Catalytic dewaxing process employing surface acidity deactivated zeolite catalysts
US5846503A (en) * 1990-12-17 1998-12-08 Mobil Oil Corporation Process for rejuvenating used alkanolamaine solutions
US5332490A (en) * 1992-09-28 1994-07-26 Texaco Inc. Catalytic process for dewaxing hydrocarbon feedstocks
US5614079A (en) * 1993-02-25 1997-03-25 Mobil Oil Corporation Catalytic dewaxing over silica bound molecular sieve
US5391286A (en) * 1993-11-03 1995-02-21 Texaco Inc. Process for catalytic dewaxing of hydrocarbon feedstocks
US5855767A (en) * 1994-09-26 1999-01-05 Star Enterprise Hydrorefining process for production of base oils
US5833837A (en) * 1995-09-29 1998-11-10 Chevron U.S.A. Inc. Process for dewaxing heavy and light fractions of lube base oil with zeolite and sapo containing catalysts
US6068757A (en) * 1995-11-03 2000-05-30 Coastal Eagle Point Oil Company Hydrodewaxing process
US6399845B1 (en) 1997-05-29 2002-06-04 Fortum Oil & Gas Oy Process for producing high grade diesel fuel
US6051129A (en) * 1998-07-24 2000-04-18 Chevron U.S.A. Inc. Process for reducing haze point in bright stock
US7077948B1 (en) * 1998-11-18 2006-07-18 Shell Oil Company Catalytic dewaxing process
US6294077B1 (en) 2000-02-02 2001-09-25 Mobil Oil Corporation Production of high viscosity lubricating oil stock with improved ZSM-5 catalyst
US6656342B2 (en) * 2001-04-04 2003-12-02 Chevron U.S.A. Inc. Graded catalyst bed for split-feed hydrocracking/hydrotreating
US6699385B2 (en) 2001-10-17 2004-03-02 Chevron U.S.A. Inc. Process for converting waxy feeds into low haze heavy base oil
EP1462168A1 (en) 2003-03-24 2004-09-29 Institut Francais Du Petrole Catalyst and its use for improving the pour point of hydrocarbon feedstocks
US7955401B2 (en) 2007-07-16 2011-06-07 Conocophillips Company Hydrotreating and catalytic dewaxing process for making diesel from oils and/or fats
US20090019763A1 (en) * 2007-07-16 2009-01-22 Conocophillips Company Hydrotreating and catalytic dewaxing process for making diesel from oils and/or fats
US9039892B2 (en) 2012-09-05 2015-05-26 Syed Tajammul Hussain Nano catalytic dewaxing of heavy petroleum wastes (>C-23 alkanes)
US20190185771A1 (en) * 2017-12-19 2019-06-20 Exxonmobil Research And Engineering Company Dewaxed diesel fuel composition
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TR17826A (en) 1976-04-13
JPS5017401A (en) 1975-02-24
DE2428463C2 (en) 1990-02-15
BE816234A (en) 1974-12-12
AU6929674A (en) 1975-11-27
FR2233384A1 (en) 1975-01-10
FR2233384B1 (en) 1979-10-12
IT1015078B (en) 1977-05-10
GB1443877A (en) 1976-07-28
NL7407870A (en) 1974-12-17
JPS5911635B2 (en) 1984-03-16
DE2428463A1 (en) 1975-01-09
CA1024091A (en) 1978-01-10
ZA742111B (en) 1975-11-26

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