US2944012A - Process for stabilizing jet fuels - Google Patents

Process for stabilizing jet fuels Download PDF

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US2944012A
US2944012A US646288A US64628857A US2944012A US 2944012 A US2944012 A US 2944012A US 646288 A US646288 A US 646288A US 64628857 A US64628857 A US 64628857A US 2944012 A US2944012 A US 2944012A
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fuel
hydrotreating
jet
product
thermally stable
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Charles E Thompson
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ExxonMobil Technology and Engineering Co
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Exxon Research and Engineering Co
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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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/06—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including a sorption process as the refining step in the absence of hydrogen
    • 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
    • C10G2400/08—Jet fuel

Definitions

  • the present invention relates to the preparation of fuels adapted to be used in internal combustion and jet engines. More particularly, the present invention relates to an improved process for the preparation of jet fuels that are thermally stable and less subject to deteriorative changes and deposit formation than are presently available by conventional preparations.
  • the military services have set up a number of jet fuel specifications in which an effort has been made to define fuels that minimize deposit formation and other difiiculties that have been encountered in the operation of jet aircraft. Specification of three such fuel types are given in Table I.
  • Jet fuels for use in commercial aircraft are normally obtained by segregating selected refinery streams boiling in the naphtha and kerosene range, preferably having substantial paraflinic content. These fuels are not stable enough for use in supersonic aircraft because of the extremely high heat stability required. Treating methods employed for stabilizing hydrocarbons for normal service have not been found satisfactory for stabilizing jet fuels. thermally stable jet fuel. Such processes are not only expensive, but entail substantial product losses and are not suited for large scale plant production.
  • thermally stable jet fuels may be prepared by treating selected hydrocarbon distillates boiling in the range of 200 to 600 F. with hydrogen in the presence of a catalyst such as cobalt molybdate, molybdenum disulfide or molybdena supported on alumina where the proportion of CoMoO M05 or M varies from 5 to 25% and the alumina or alumina-silica base varies from 95 to 75%.
  • a catalyst such as cobalt molybdate, molybdenum disulfide or molybdena supported on alumina where the proportion of CoMoO M05 or M varies from 5 to 25% and the alumina or alumina-silica base varies from 95 to 75%.
  • the temperature is in'the range of 300-750 F.
  • the pressure may be in the range of 50-1000 p.s.i.g.
  • the feed rate may be varied from 0.5 to v./hr./v.
  • the amount of hydrogen may vary from 50-6000 s.c.
  • the product flom this treatment is then either stripped with nitrogen or other inert gas, or caustic washed to remove hydrogen sulfide, or both, and treated with an adsorbent material such as activated diatomaceous earth or other Only servere acid treating has produced a adsorbent material such as activated carbon or alumina.
  • the oil is treated with 1.0 to 10% by weight of the adsorbent material.
  • the jet fuel is then separated from the adsorbent material by decanting, filtering or centrifuging.
  • the resulting jet fuel is exceptionally thermally stable.
  • -a selected petroleum feedstock containing hydrocarbons which boil in the heavy naphtha and kerosene range is passed via line 2 to a conventional hydrotreating unit 4, and is there treated with hydrogen under the conditions enumerated heretofore.
  • the hydrotreating catalysts that-can be employed in the hydrofining include 5-15% molybdena oxide on activated alumina, mixtures of cobalt oxides (2-6 Wt. percent) and molybdenum oxides (6-15 wt. percent), an equivalent amount of cobalt molybdate on activated alumina, and other sulfur resistant hydrogenation catalysts such as those of the nickel tungsten sulfide type and unsupported molybdenum disulfide.
  • Regeneration of the fixed bed catalyst may be required periodically, depending largely upon the nature of the feed stock. This regeneration is conveniently carried out at a temperature of about 750-1000 F., with an oxygencontaining gas.
  • the oil and hydrogen are contacted with catalyst by continuous flow through vessel 4 packed with catalyst.
  • the oil feed to the reactor is preheated to the required temperature by means of a furnace or similar means.
  • Hydrogen may or may not be heated prior to feeding to the reactor depending on the quantity used.
  • the degree of' contact of oil saturated with hydrogen with the catalyst is determined by the ratio of the oil flow rate to the catalyst volume.
  • hydrotreated product may be caustic washed to remove acidic sulfur.
  • the sulfur-free hydrocarbon product, cooled to a temperature belowabout 100 F. in cooler 12 is passed via line 10 to an adsorption zone 14.
  • zone 14 the liquid is contacted in a slurry with 1 to' of an adsorbent.
  • the temperature in zone 14 is in therange of 60 to 100 'F.
  • substantially any high surface area adsorbenu suchas activated diatomaceous earth, other siliceous material, char, alumina, zeolites and the like, may be employed.
  • the oil may be treated with 1.0 to 10% by weight of the adsorbent.
  • the hydrotreating step is carried out with a low surface area catalyst having good hydrogenation activity.
  • Normal treating catalyst may contain from .75 to alumina or silica alumina base.
  • This material is active as an isomerizing agent for 7 hydrocarbon materials and capable at the temperatures employed of forming hydrocarbon products which. will 7 polymerize and, therefore, be less thermally stable than before treating as for example, the isomerization and dehydrogenation of tetralin to methyl-indene.
  • Use of a catalyst having a very low surface area'and not contain: ing alumina or silica avoids thisreaction.
  • Such catalysts as unsupported molybdenum disulfide or nickel tungsten' sulfide are superior for hydrotreating a jet fuel for thermal stability for two reasons. They do not have the isomerization activity of alumina supported catalysts and they have greater hydrogenation activity.
  • hydrotreating catalyst at a temperature of from about- 300750 F., and pressure of 50-1000 p.s.i.g., removing 7 sulfur-containing products from said hydrotreating material, condensing said hydro treated product, treating said liquefied product with an adsorbent having a high surface area, and recovering a thermally stable fuel.
  • An] improved process for preparing a thermally stable jet fuel which comprises hydrot reating a predominantly paraflinic hydrocarbon fraction containing sulfur and boiling in the heavy naphtha and kerosene range in the presence of an unsupported hydrotreating catalyst at hydrotreating conditions of temperature and pressure,
  • hydrotreated prod- Y 110 is caustic scrubbed.

Description

July 5, 1960 C. E. THOMPSON PROCESS FOR STABILIZING JET FUELS HYDROTREATING EL. ZONE Filed March 15, 1957 PURGE GAS STRIPPER ADSORPTlON ZONE- l4 PURGE GAS 1 Chorles'E. Thorhpsoh Inventor By a 1 a Patent Attorney United States. Patent PROCESS FOR STABILIZING FUELS Charles E. Thompson, Fanwood, N.J., assignor to Esso Research and Engineering Company, a corporation of Delaware Filed Mar. 15, 1957, Ser. No. 646,288
8 Claims. (Cl. 208-212) The present invention relates to the preparation of fuels adapted to be used in internal combustion and jet engines. More particularly, the present invention relates to an improved process for the preparation of jet fuels that are thermally stable and less subject to deteriorative changes and deposit formation than are presently available by conventional preparations.
In the operation of both internal combustion and jet engines, a serious problem existing at the present time is the formation of engine deposits, in which fuels play an important role. Furthermore, particularly in jet engines, a further problem arises in the plugging of fuel filters at low temperatures. Carbonaceous deposits in the combustors of a jet engine are very undesirable in that they disrupt the desired fuel spray patterns in the combustors, cause warping of the liners and thus reduce the amount of power that can be generated. Furthermore, jet fuels must be thermally stable as they are circulated through a heat exchanger with the oil from the engine; if unstable constituents are present, the heat exchangers, screens and nozzles in the fuel system become clogged with the polymeric material formed, thus causing malfunctioning of the engine.
The military services have set up a number of jet fuel specifications in which an effort has been made to define fuels that minimize deposit formation and other difiiculties that have been encountered in the operation of jet aircraft. Specification of three such fuel types are given in Table I.
Jet fuels for use in commercial aircraft are normally obtained by segregating selected refinery streams boiling in the naphtha and kerosene range, preferably having substantial paraflinic content. These fuels are not stable enough for use in supersonic aircraft because of the extremely high heat stability required. Treating methods employed for stabilizing hydrocarbons for normal service have not been found satisfactory for stabilizing jet fuels. thermally stable jet fuel. Such processes are not only expensive, but entail substantial product losses and are not suited for large scale plant production.
It has now been found that highly satisfactory thermally stable jet fuels may be prepared by treating selected hydrocarbon distillates boiling in the range of 200 to 600 F. with hydrogen in the presence of a catalyst such as cobalt molybdate, molybdenum disulfide or molybdena supported on alumina where the proportion of CoMoO M05 or M varies from 5 to 25% and the alumina or alumina-silica base varies from 95 to 75%. In this step the temperature is in'the range of 300-750 F., the pressure may be in the range of 50-1000 p.s.i.g., the feed rate may be varied from 0.5 to v./hr./v. and the amount of hydrogen may vary from 50-6000 s.c.f./b. The product flom this treatment is then either stripped with nitrogen or other inert gas, or caustic washed to remove hydrogen sulfide, or both, and treated with an adsorbent material such as activated diatomaceous earth or other Only servere acid treating has produced a adsorbent material such as activated carbon or alumina.
2,944,032 Patented July 5, 1960 TABLE 1 MIL-F-5624O SIP-4 .TP-5
Gravity, API Freezing Point, F "max" Aromatics, Vol. Percent Oleflns, Vol. Percent..- Smoke Vol. Index Smoke Point, mm Existant Gum, mg./ 1111.. Potential Gum, mg./100 ml. Sulfur, Total Wt. Peroent- Mercaptan Sulfur, Wt. Percen Flash Point, F Heating Value, Net B.t.u./lb
r Aniline-Gravity Product m1n.- Reid Vapor Pressure, p at Water Tolerance, ml Corrosion, Copper Strip 20 max 7 7 6 max- 10 Lt. Tan
1 0r pass doctor test.
Mar. pressure drop in CFR fuel eoker after 5 hours at. 6#/hr. full flow-rate, 400,F. fuel temperature, 500 F. filter temperature. Equivalent to a merit rating of 510.
The oil is treated with 1.0 to 10% by weight of the adsorbent material. The jet fuel is then separated from the adsorbent material by decanting, filtering or centrifuging. The resulting jet fuel is exceptionally thermally stable.
In accordance with the flow sheet of the present invention, -a selected petroleum feedstock containing hydrocarbons which boil in the heavy naphtha and kerosene range is passed via line 2 to a conventional hydrotreating unit 4, and is there treated with hydrogen under the conditions enumerated heretofore.
The hydrotreating catalysts that-can be employed in the hydrofining include 5-15% molybdena oxide on activated alumina, mixtures of cobalt oxides (2-6 Wt. percent) and molybdenum oxides (6-15 wt. percent), an equivalent amount of cobalt molybdate on activated alumina, and other sulfur resistant hydrogenation catalysts such as those of the nickel tungsten sulfide type and unsupported molybdenum disulfide.
Regeneration of the fixed bed catalyst may be required periodically, depending largely upon the nature of the feed stock. This regeneration is conveniently carried out at a temperature of about 750-1000 F., with an oxygencontaining gas.
In the hydrotreating operation, the oil and hydrogen are contacted with catalyst by continuous flow through vessel 4 packed with catalyst. The oil feed to the reactor is preheated to the required temperature by means of a furnace or similar means. Hydrogen may or may not be heated prior to feeding to the reactor depending on the quantity used. The degree of' contact of oil saturated with hydrogen with the catalyst is determined by the ratio of the oil flow rate to the catalyst volume.
From hydrotreating zone 4 the liquid is passed via line 6 to stripper 8 to remove residual H 8, which is an undesirable constituent in jet fuels. Alternatively or in addition, the hydrotreated product may be caustic washed to remove acidic sulfur. The sulfur-free hydrocarbon product, cooled to a temperature belowabout 100 F. in cooler 12 is passed via line 10 to an adsorption zone 14.
. It isimportant that adsorption be carried out in the liquid phase. Vapor phase adsorption will not provide the thermally stable jet fuel. In zone 14 the liquid is contacted in a slurry with 1 to' of an adsorbent. The temperature in zone 14 is in therange of 60 to 100 'F., and
' substantially any high surface area adsorbenusuchas activated diatomaceous earth, other siliceous material, char, alumina, zeolites and the like, may be employed. The oil may be treated with 1.0 to 10% by weight of the adsorbent. a
The jet fuel is then separated from the adsorbent material by decantation, filtration or centrifuging and is withdrawn through line 16. 'Theresulting fuel is thermally stable." 7 a a 7 a a The advantages of the present invention will be better understood by reference to the following examples:
Exa mp le Specifications defining'the'necessary levels of thermal stability of jet fuel which Lcanibe determined on a labora-. tory scale are based on the CFR fuel coker rig, a device for measuring fuel thermal stability. High stability jet fuelsfo'f the JP-j-Sj aind JP-6' typqhave a specification of a CFR fuel coker merit ratingof500. The CFR fuel coker is essentially a scaled down version of a full scale turbo engine fuel system which simulates the fuel/oil heat exchanger and combustor nozzle of a jet engine. Fuel is pumped at predetermined rates through a hot heat- The substantially improved-product employing the combinationsteps is immediately apparent; Thus it can be seen from the above table that the individual treating steps described have not been effective in producing a thermally stable jet fuel. Evenon the kerosene which had a 230 merit rating untreated it was necessary to use an oleum treat of 59 lb./bbl. to obtain a stable fuel.
Even higher acid treating'would be necessary to stabilize the other sample of kerosene. These high acid treats are expensive and not suited to large scale plant production! 0 Example 2 v To demonstrate the-importance of liquid phase adsorption, further experimental work was carried out "'1 rating of this fuel was only 405, a value lower than'spe'ciexchanger tube which simulates the hot fuel line sections of the engine. The fuel then passes through a heated 20 micron metal filter section wlgrich represents the nozzle area orsmall fuel passages in the hot section of the engine where fuel degradation products may become trapped. Thefilter traps. fuel degradation products formed during the test. Fuel degradation is measured by the increased pressure drop across the metal filter and by a'visualrat- .ing of the varnish-likedeposits laid down on the hot heat exchanger .tube.- Typical pressure drop data are translated into an arbitrary merit rating.
A- series of tests were carried out whereinKa) a distillate fuel boiling in the range of 345 to 512. F., having an API gravity of 42.4 at 60 F. and a freezing point of 48 a F., was hydrotreated in the presence of a cobalt molybobtained:
EXPERIMENTAL PROCESS TO IMPROVE THERMAL STABILITY OFR Fuel Coker 1 Process Merit Tube Rating Deposits Targ 500 Clean to Lt.
Tan.
Untreated ZIP-5 Stock 10 Fail.
Hydrotreated 235-535 Variable.
3 Wt. Percent Clay Contact 300 Fail.
Oxidized (Air at 170 F.). 160 Fall.
Sodium Treating 415 Pass.
SO; Extracted 300 Fall.
Hydrotreated+3 Wt. Percent Clay 850 Pass.
Contact. 7
Untreated JP-5v Stock 230 Fall;
Hydrotr eating V 405 3% Oleum (19. .lbbl 355 9% Oleum (591b./bbl.)-.- 550 Hydrotreating+3 Wt. Percent Cla 700 Pass.
Contact. V
' 1 High temperature test condition's:;400 F. fuel temperature; 500 F.
filter temperature; 6'1b./hr..fue1 now.
R 1 hr. of stirring with Super Filtrol at 74 11. V7
wherein the same 'feed'was hydrotreated in the presence of a cobalt-molybdate on alumina catalyst at 565 3.7 v./hr./v., 3500 -s.c.f. of l-l /barrehat .750 psig The total product from the hydrotreating step was passed directly to the adsorption 'stagewhere the conditions were 480 F., a feed rate of 5.5 v./ hr./v.,'and a pressure of 0.-;p.s.i.g.
Theproduct from" this experimentwas evalnatedlby the CFR fuel coker rig test for thermal stability. The
fication forjet fuel and considerably lower than the850 rating obtained by-the process of the present invention.
I d-another modification of the present invention, the hydrotreating step is carried out with a low surface area catalyst having good hydrogenation activity. Normal treating catalyst may contain from .75 to alumina or silica alumina base.
This material is active as an isomerizing agent for 7 hydrocarbon materials and capable at the temperatures employed of forming hydrocarbon products which. will 7 polymerize and, therefore, be less thermally stable than before treating as for example, the isomerization and dehydrogenation of tetralin to methyl-indene. Use of a catalyst having a very low surface area'and not contain: ing alumina or silica avoids thisreaction. Such catalysts as unsupported molybdenum disulfide or nickel tungsten' sulfide are superior for hydrotreating a jet fuel for thermal stability for two reasons. They do not have the isomerization activity of alumina supported catalysts and they have greater hydrogenation activity. The greater hydrogenation activity is beneficial in that the hydrogenated products-have a lowered smoking tendency' This is a characteristic that is to be desired in jet fuels. What'is claimed is: 1. An improved process for refining a hydrocarbon fuel to produce a highly thermally stable product which comprises segregating a refining stream boiling in the range of about 200-600" F. and containing sulfur, catalytically hydrotreating said stream in the presence. ofa
hydrotreating catalyst at a temperature of from about- 300750 F., and pressure of 50-1000 p.s.i.g., removing 7 sulfur-containing products from said hydrotreating material, condensing said hydro treated product, treating said liquefied product with an adsorbent having a high surface area, and recovering a thermally stable fuel.
2. The process of claim 1 wherein said catalyst is a molybdenum compound.
3. The process of claim 1, wherein said hydrotreated product is cooled to at least v F. prior to treatment withrsaid adsorbent. v
'4. The process of claim 3 wherein said adsorbent is a diatomaceous earth.
5. The process of claim 3. wherein said adsorbent is a clay.
6. An] improved process for preparing a thermally stable jet fuel which comprises hydrot reating a predominantly paraflinic hydrocarbon fraction containing sulfur and boiling in the heavy naphtha and kerosene range in the presence of an unsupported hydrotreating catalyst at hydrotreating conditions of temperature and pressure,
cooling said hydrotreated product to at least 100 F., and treating said product at a temperature of about 60100 F., in the liquid phase with 1 to 10% by weight of an adsorbent having a high surface area.
7. The process of claim 6 wherein said scrubbing is by an inert gas.
8. The process of claim 6 wherein hydrotreated prod- Y 110: is caustic scrubbed.
UNITED STATES PATENTS Murray et a1. Sept. 6, 1955 Fenske et a1. Oct. 9, 1956 Annable et a1. Nov. 6, 1956 Scovill et al. July 16, 1957

Claims (1)

1. AN IMPROVED PROCESS FOR REFINING A HYDROCARBON FUEL TO PRODUCE A HIGHLY THERMALLY STABLE PRODUCT WHICH COMPRISES SEGREGATING A REFINING STREAM BOILING IN THE RANGE OF ABOUT 200-300*F. AND CONTAINING SULFUR, CATALYTICALLY HYDROTREATING SAID STREAM IN THE PRESENCE OF A HYDROTREATING CATALYST AT A TEMPERATURE OF FROM ABOUT 300-750* F., AND PRESSURE OF 50-1000 P.S.I.G., REMOVING SULFUR-CONTAINING PRODUCTS FROM SAID HYDROTREATING MATERAIL, CONDENSING SAID HYDROTREATED PRODUCT, TREATING SAID LIQUENFIED PRODUCT WITH AN ADSORBENT HAVING A HIGH SURFACE AREA, AND RECOVERING A THERMALLY STABLE FUEL.
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Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3039957A (en) * 1960-02-09 1962-06-19 Exxon Research Engineering Co Production of solvents
US3044955A (en) * 1958-06-03 1962-07-17 Shell Oil Co Electrical insulating oils
US3121678A (en) * 1960-02-09 1964-02-18 Exxon Research Engineering Co Production of specialty oil
US4719007A (en) * 1986-10-30 1988-01-12 Uop Inc. Process for hydrotreating a hydrocarbonaceous charge stock
WO2009070561A1 (en) 2007-11-30 2009-06-04 Saudi Arabian Oil Company Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds
US20090145808A1 (en) * 2007-11-30 2009-06-11 Saudi Arabian Oil Company Catalyst to attain low sulfur diesel
US20090230026A1 (en) * 2008-02-21 2009-09-17 Saudi Arabian Oil Company Catalyst To Attain Low Sulfur Gasoline
US20110024330A1 (en) * 2006-12-06 2011-02-03 Saudi Arabian Oil Company Composition and Process for the Removal of Sulfur from Middle Distillate Fuels
US8535518B2 (en) 2011-01-19 2013-09-17 Saudi Arabian Oil Company Petroleum upgrading and desulfurizing process
US9005432B2 (en) 2010-06-29 2015-04-14 Saudi Arabian Oil Company Removal of sulfur compounds from petroleum stream
US10526552B1 (en) 2018-10-12 2020-01-07 Saudi Arabian Oil Company Upgrading of heavy oil for steam cracking process
US10703999B2 (en) 2017-03-14 2020-07-07 Saudi Arabian Oil Company Integrated supercritical water and steam cracking process
US10752847B2 (en) 2017-03-08 2020-08-25 Saudi Arabian Oil Company Integrated hydrothermal process to upgrade heavy oil

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US2717230A (en) * 1951-06-19 1955-09-06 Universal Oil Prod Co Catalytic reforming of hydrocarbon charge stocks high in nitrogen compounds
US2766179A (en) * 1954-05-03 1956-10-09 Universal Oil Prod Co Hydrocarbon conversion process
US2769762A (en) * 1953-08-31 1956-11-06 Pure Oil Co Production of naphthas of improved characteristics by treating with bauxite
US2799718A (en) * 1954-10-18 1957-07-16 Standard Oil Co Odorless solvent and method of making same

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2717230A (en) * 1951-06-19 1955-09-06 Universal Oil Prod Co Catalytic reforming of hydrocarbon charge stocks high in nitrogen compounds
US2769762A (en) * 1953-08-31 1956-11-06 Pure Oil Co Production of naphthas of improved characteristics by treating with bauxite
US2766179A (en) * 1954-05-03 1956-10-09 Universal Oil Prod Co Hydrocarbon conversion process
US2799718A (en) * 1954-10-18 1957-07-16 Standard Oil Co Odorless solvent and method of making same

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3044955A (en) * 1958-06-03 1962-07-17 Shell Oil Co Electrical insulating oils
US3121678A (en) * 1960-02-09 1964-02-18 Exxon Research Engineering Co Production of specialty oil
US3039957A (en) * 1960-02-09 1962-06-19 Exxon Research Engineering Co Production of solvents
US4719007A (en) * 1986-10-30 1988-01-12 Uop Inc. Process for hydrotreating a hydrocarbonaceous charge stock
US20110024330A1 (en) * 2006-12-06 2011-02-03 Saudi Arabian Oil Company Composition and Process for the Removal of Sulfur from Middle Distillate Fuels
US8323480B2 (en) 2006-12-06 2012-12-04 Saudi Arabian Oil Company Composition and process for the removal of sulfur from middle distillate fuels
US20090145807A1 (en) * 2007-11-30 2009-06-11 Saudi Arabian Oil Company Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds
US8142646B2 (en) 2007-11-30 2012-03-27 Saudi Arabian Oil Company Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds
US20090145808A1 (en) * 2007-11-30 2009-06-11 Saudi Arabian Oil Company Catalyst to attain low sulfur diesel
WO2009070561A1 (en) 2007-11-30 2009-06-04 Saudi Arabian Oil Company Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds
US20090230026A1 (en) * 2008-02-21 2009-09-17 Saudi Arabian Oil Company Catalyst To Attain Low Sulfur Gasoline
US10252247B2 (en) 2008-02-21 2019-04-09 Saudi Arabian Oil Company Catalyst to attain low sulfur gasoline
US10596555B2 (en) 2008-02-21 2020-03-24 Saudi Arabian Oil Company Catalyst to attain low sulfur gasoline
US9636662B2 (en) 2008-02-21 2017-05-02 Saudi Arabian Oil Company Catalyst to attain low sulfur gasoline
US9005432B2 (en) 2010-06-29 2015-04-14 Saudi Arabian Oil Company Removal of sulfur compounds from petroleum stream
US9951283B2 (en) 2011-01-19 2018-04-24 Saudi Arabian Oil Company Petroleum upgrading and desulfurizing process
US8535518B2 (en) 2011-01-19 2013-09-17 Saudi Arabian Oil Company Petroleum upgrading and desulfurizing process
US10752847B2 (en) 2017-03-08 2020-08-25 Saudi Arabian Oil Company Integrated hydrothermal process to upgrade heavy oil
US11149216B2 (en) 2017-03-08 2021-10-19 Saudi Arabian Oil Company Integrated hydrothermal process to upgrade heavy oil
US10703999B2 (en) 2017-03-14 2020-07-07 Saudi Arabian Oil Company Integrated supercritical water and steam cracking process
US11149218B2 (en) 2017-03-14 2021-10-19 Saudi Arabian Oil Company Integrated supercritical water and steam cracking process
US10526552B1 (en) 2018-10-12 2020-01-07 Saudi Arabian Oil Company Upgrading of heavy oil for steam cracking process
US10975317B2 (en) 2018-10-12 2021-04-13 Saudi Arabian Oil Company Upgrading of heavy oil for steam cracking process
US11230675B2 (en) 2018-10-12 2022-01-25 Saudi Arabian Oil Company Upgrading of heavy oil for steam cracking process

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