US3775291A - Production of jet fuel - Google Patents

Production of jet fuel Download PDF

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Publication number
US3775291A
US3775291A US00177439A US3775291DA US3775291A US 3775291 A US3775291 A US 3775291A US 00177439 A US00177439 A US 00177439A US 3775291D A US3775291D A US 3775291DA US 3775291 A US3775291 A US 3775291A
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process according
feed
mixture
liquid
zone
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US00177439A
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Yuan Sze M Chuan
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CB&I Technology Inc
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Lummus Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
    • B01J8/0449—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
    • B01J8/0453—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
    • 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

  • Jet fuel particularly suitable for use in supersonic air- [5 l 1 hit Cl IIIIIIIIIIIIII H 23/00 craft, is produced from a mixture of a petroleum frac- [58] Fieid 208515 57 tion boiling substantially in the kerosene range and a mixture of branched chain olefinic hydrocarbons having an average of nine to 16 carbon atoms per mole- [56] References cued cule. The mixture is passed through two hydrogena- UNITED STATES PATENTS tion zones in series, co-currently with hydrogen in the 2,594,302 1971 first, countercurrent to hydrogen in the second.
  • jet fuel To be suitable for use in such aircraft, jet fuel must meet specifications exceeding in certain respects, those for jet fuel whichcan be used in ordinary, subsonic aircraft. Particularly, jet fuel, to be used for supersonic aircraft, must meet standards of low freezing point and high luminometer number.
  • the luminometer number is a measure of the burning characteristics of a fuel. The higher the number, the less smoke produced by the fuel during take-off and the lower the amount of radiation produced by the flame. This number is determined by the method described in ASTM designation D1 322-54T.
  • a high luminometer number is associated with low aromatics and also means at high smoke point.
  • the fuels produced by this invention are not suitable for use only in supersonic aircraft. They are, in general, aviation turbine fuels of a high quality, which more than meet the specifications of fuels for use in jets flying below Mar. 1, as well as those which fly at supersonic speeds.
  • this invention contemplates the production of jet fuels by a process comprising:
  • FIGURE is a diagrammatic illustration of the process of this invention.
  • the hydrogenation zones are preferably contained in one hydrogenation vessel, which has the form of a vertical cylinder having dished ends and pressure sustaining walls.
  • the interior of the vessel is divided by horizontal partitions 12, 14, and 24, which are preferably perforated or foraminous plates or the like, into a plurality of chambers or zones including an upper reaction chamber 16, an intermediate vapor-disengaging zone 20, and a lower reaction chamber 18.
  • the reaction chambers 16 and 18 are packed with a suitable hydrogenation catalyst 22, which may be of any of the well known hydrogenation-dehydrogenation catalysts, including such as Raney nickel, or nickel, platinum or palladium, preferably on a support such as alumina, silica, kieselguhr, diatomaceous earth, magnesia, zirconia or other inorganic oxides, alone or in combination.
  • a suitable hydrogenation catalyst 22 which may be of any of the well known hydrogenation-dehydrogenation catalysts, including such as Raney nickel, or nickel, platinum or palladium, preferably on a support such as alumina, silica, kieselguhr, diatomaceous earth, magnesia, zirconia or other inorganic oxides, alone or in combination.
  • the catalyst in zone 16 is supported on partition 12.
  • the catalyst in zone 18 is supported on a similar partition 24. Partition 24 is preferably spaced somewhat above the bottom of the converter, thus defining the upper boundary of an additional lower chamber or zone 26
  • mixture of branched chain olefins as hereinafter described, in an amount of 10-50 volume percent, preferably 15-40 percent, based on the aromatics-containing feed.
  • the combined feed proceeds through line 46, and into it is introduced a hydrogen stream from line 38; it then proceeds through line 40 as indicated by the arrows, until it joins line 44, from which is added a condensed recycle liquid from separator 34.
  • the resulting mixture of feed, recycle and hydrogen then passes through line 42 into the first zone 16 of the hydrogenation vessel which is operated at a temperature of from about 200F. to about 500F., and a pressure of from about 400 to about 1,500 psi.
  • the mixture of feed recycle liquid and hydrogen passes downwardly through the catalyst bed in zone 16, under adiabatic reaction conditions in which a substantial amount of the aromatics are hydrogenated to the corresponding naphthenic compounds, and substantially all of the olefins are also hydrogenated to the corresponding isoparaffins.
  • the reaction product which passes out of zone 16 is a two-phase mixture.
  • the liquid phase is a mixture of saturated and some unsaturated compounds.
  • the gas phase effluent is a mixture of hydrogen, inert gaseous impurities, and vaporized liquid hydrocarbons of a composition generally similar to that of the liquid phase effluent.
  • the liquid phase of the effluent passes downwardly through the vapor-disengaging zone into the second hydrogenation zone 18 (through partition 14, which serves as a distributor plate).
  • reaction zone 18 hydrogen introduced through line 48 and passing through chamber 26 contacts the liquid phase effluent countercurrently, completing the hydrogenation of the aromatics.
  • the hydrogen is introduced without being preheated, at a relatively low tem perature, compared to that of the liquid phase effluent from zone 16, generally the hydrogen temperature is no higher than about l00-l20F.
  • the liquid portion which emerges from hydrogenation zone 18 is briefly accumulated in chamber 26, permitting disengagement of the vapors and sealing the outlet to line 50 to prevent escape of hydrogen.
  • the liquid portion is collected in line 50, and contains a very minor portion, generally less than 1 volume percent, of residual unhydrogenated aromatics, and virtually no olefins.
  • the gas phase effluent from reaction zone 18 contains excess hydrogen, inert gaseous impurities and vaporized hydrocarbons similar to those produced in the gas phase effluent from zone 16.
  • the gas phase effluents from both the first hydrogenation zone 16 and the second hydrogenation zone 18 collect in vapor-disengaging zone 20.
  • the combined gas phase fraction is withdrawn through line 28, and first passed through heat exchanger or waste heat boiler 52, in which some of the heat is used to produce steam for use in other processing steps, or in other processes, or for general purposes.
  • the still hot vapor mixture is then passed through line 54, then preferably through condenser 32, where the vaporized liquid phase components remaining in the system are recondensed to liquids.
  • the resulting two-phase system consisting of gaseous hydrogen, inert gases, and reliquefied hydrocarbons, is passed into separator 34, where the liquid and gaseous phases are separated.
  • the liquid phase is passed through line 44 to be mixed with the feed to hydrogenation zone 16 as previously described.
  • the gaseous phase comprising hydrogen and inert gases, may be vented partially, as through line 56, to prevent build-up of inert impurities in the system.
  • Fresh feed hydrogen gas may be supplied from line 48 through line 58 into the recycle gas, in the event that the recycle hydrogen is insufficient to supply the needs in the first hydrogenation zone.
  • An important feature of this invention is a built-in temperature control. Reactions of the type contemplated are exothermic. The production of the desired jet fuel is favored by low outlet temperatures. Furthermore, runaway reactions must be prevented or coke and undesirable side products will be formed. Accordingly, external temperature control means are usually necessitated in processes for hydrogenating aromatics for jet fuel production. The present process, however, provides an inherent temperature control, particularly in the second hydrogenation zone 18. As the hydrogen feed from line 48 passes upwardly through this zone, a portion of the heat present in that chamber is absorbed in the process of sensibly heating the hydrogen.
  • the vaporized hydrocarbons recovered from the vapor disengaging zone 20 and used as recycle comprise partially hydrogenated feed containing up to about 5 percent aromatics.
  • the volume ratio of recycle to fresh feed is generally in the range of about 0.25: l .0 to about l.5:l.0, and depends on a number of factors, including hydrogen partial pressure and purity, desired temperature in the reactor, etc.
  • the major portion of the feed to this process comprises a petroleum fraction generally boiling in the kerosene range, particularly in the range from about 300F. to about 550F.
  • This portion of the feed may be a straight run kerosene, heavy naphtha, furnace oil, catalytically cracked cycle oil, etc.
  • the process of this invention does not accomplish desulfurization for practical purposes, though some desulfurization may take place; consequently most feeds should be desulfurized prior to being introduced into the process, generally in a separate unit (not shown).
  • the olefinic mixture utilized in the process of this invention is a medium molecular weight oligomer of propylene or of butene isomers, or a mixed oligomer of C to C olefins.
  • the oligomer being a polymer of olefins is itself unsaturated, and will contain nine to 16 carbon atoms per molecule. Most preferable are C, -C, olefinic compounds, with those having a greater degree of branching being especially preferred.
  • these oligomers and their mixtures boil in the range of about 280 to about 525F., preferably 340 to about 500F.
  • Such oligomers as propylene trimer and tetramer, butene trimmers and tetramers, and mixed propylene-butene and ethylene-propylenebutene oligomers are suitable, as are mixtures such as polymer gasoline.
  • Oligomers of butenes, or of butenes with ethylene and/or propylene are expected to be particularly suitable, as these will display the greatest tendency toward forming branched chains.
  • the kerosene portion of the feed has undergone desulfurization just prior to its admission into the first hydrogenatiori zone, it will be sufficiently hot that no further heating is required to bring it up to reaction temperature. If, however, it has been obtained from a simple fractionation process or has been allowed to cool down prior to being passed into this process, preheating is required. In any case, the hydrogen fed to the first hydrogenation zone 16 must be preheated prior to its introduction into this zone. The liquid recycle to this zone must also be preheated.
  • the hydrogenation of the olefinic oligomers is also an exothermic reaction, and occurs readily at somewhat lower temperatures than the hydrogenation of the kerosene feed, which generally requires an inlet temperature of at least 350 to 380F. Consequently, a saving in cost can be achieved, and the chance of over-reaction minimized when the mixed feed is introduced into the reactor at a lower temperture, generally from about 200 to about 350F. preferably 225F. to 325F.
  • the maximum temperature leaving the first reaction zone generally is limited to 575F.
  • the exothermicity of the hydrogenation of the olefins will raise the temperature of the feed part waythrough the first reaction zone 16 and thus trigger the hydrogenation of the kerosene feed. Thus, if the kerosene feed does not require preheating, the olefinic feed can be mixed with it, without requiring preheating of the olefins.
  • the preheating of the hydrogen, recycle liquid, and feed if necessary can be accomplished in a number of ways, and canbe performed separately or in the same operation and equipment.
  • a convenient method, in this process is to utilize the heat contained in the vapors in lines 28 and 54, which have been removed from the vaper-disengaging zone 20.
  • the combined hydrogen (and feed, if necessary) in stream 42, together with recycle liquid from line 44, is passed through heat exchanger 30, in which it is preheated to the desired inlet temperature by indirect heat exchange with the partially cooled vapors in line 54.
  • This heat exchange under some conditions, may have the additional effect of partially condensing some of the hydrocarbons in the combined vapor stream, facilitating the separation of hydrocarbons for recycle from the hydrogen and other gases, in separator M.
  • the fresh kerosene feed if it is already sufficiently hot so as not to require preheating, it should be by-passed around the preheater in a conventional manner to avoid overheating and undesirable side reactions.
  • the fresh kerosene feed will then enter the system through line 43 instead of through line 46.
  • Olefinic feed can be mixed from line 411.. In this case, only the hydrogen and recycled liquid hydrocarbons will be preheated.
  • the preheating of the fresh feed, liquid recycle and hydrogen can be done in separate heat exchangers, and the heated materials mixed before being introduced into the reactor.
  • This separate preheating can be done using any source of available heat, including the hot vapor mixture in line 54.
  • the ratio of hydrogen to fresh feed in the mixture fed to reaction zone 16 may vary from a minimum of the .stoichiometric ratio of moi for each double bond to as much as about 3 mols for each double bond, and the ratio of hydrogen in line 48 to the liquid material entering reaction zone 18 may vary from about 0.3 to about 1.0 moles/mole.
  • the L.H.S.V. in the first zone 16 is preferably maintained between about 0.5 and about 6.0, based on fresh feed, while that in the second section 18 is generally at a higher level.
  • the temperature conditions in the second section should be adjusted to maintain the temperature of the liquid product at the outlet 50 between about 250F and about 450F, preferably between about 300F. and about 400F., to provide optimum conditions favoring hydrogenation of the aromatics to naphthenes and close equilibrium approach.
  • the Smoke Point of the mixed kerosene-propylene tetramer feed was 22.3 min and the luminometer number 50 min.
  • the reactor was operated at an inlet temperature (zone 16) of 417F., a total pressure of 900 psig. and an overall L.H.S.V. of 1.83.
  • the overall ratio of hydrogen to fresh feed hydrocarbons was 700 S.C.F. per barrel of feed.
  • the product of the reaction contained 1.3 volume percent of unsaturated aromatics, had a freezing point of 58F., a Smoke Point of 34.6 mm. and a luminometer number of 86.
  • a process for producing jet fuel comprising the steps of:
  • volume ratio of recycled liquid to fresh feed is between 0.25:1.0 and l.5:l.0.
  • step (a) A process according to claim 1 in which the petroleum fraction boiling substantially in the kerosene range is subjected to desulfurization prior to mixing in step (a).
  • step (a) A process according to claim 1 in which the petroleum fraction boiling substantially in the kerosene range. is mixed in step (a) with a mixture of branched chain olefinic hydrocarbons having an average of from 12 to 16 carbon atoms per molecule.
  • step (e) A process according to claim 1 wherein a liquid phase effluent is produced in step (e), which possesses a freezing point below 57F.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Liquid Carbonaceous Fuels (AREA)
US00177439A 1971-09-02 1971-09-02 Production of jet fuel Expired - Lifetime US3775291A (en)

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US (1) US3775291A (ja)
JP (1) JPS5418281B2 (ja)
AU (1) AU469396B2 (ja)
CA (1) CA981201A (ja)
DE (1) DE2242330A1 (ja)
ES (1) ES406278A1 (ja)
FI (1) FI60228C (ja)
FR (1) FR2151058B1 (ja)
GB (1) GB1401515A (ja)
IT (1) IT962256B (ja)
NL (1) NL176582C (ja)

Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4102778A (en) * 1975-04-10 1978-07-25 Ruether John A Method and apparatus for carrying out hydrogenation reactions
US5183556A (en) * 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
WO1998007808A1 (en) * 1996-08-23 1998-02-26 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US5882505A (en) * 1997-06-03 1999-03-16 Exxon Research And Engineering Company Conversion of fisher-tropsch waxes to lubricants by countercurrent processing
US5888376A (en) * 1996-08-23 1999-03-30 Exxon Research And Engineering Co. Conversion of fischer-tropsch light oil to jet fuel by countercurrent processing
US5928497A (en) * 1997-08-22 1999-07-27 Exxon Chemical Pateuts Inc Heteroatom removal through countercurrent sorption
US5942197A (en) * 1996-08-23 1999-08-24 Exxon Research And Engineering Co Countercurrent reactor
US6037510A (en) * 1997-05-12 2000-03-14 Basf Aktiengesellschaft Catalytic gas-phase hydrogenation of olefins
US6241952B1 (en) 1997-09-26 2001-06-05 Exxon Research And Engineering Company Countercurrent reactor with interstage stripping of NH3 and H2S in gas/liquid contacting zones
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US6495029B1 (en) 1997-08-22 2002-12-17 Exxon Research And Engineering Company Countercurrent desulfurization process for refractory organosulfur heterocycles
US6497810B1 (en) 1998-12-07 2002-12-24 Larry L. Laccino Countercurrent hydroprocessing with feedstream quench to control temperature
US6514403B1 (en) * 2000-04-20 2003-02-04 Abb Lummus Global Inc. Hydrocracking of vacuum gas and other oils using a cocurrent/countercurrent reaction system and a post-treatment reactive distillation system
US6569314B1 (en) 1998-12-07 2003-05-27 Exxonmobil Research And Engineering Company Countercurrent hydroprocessing with trickle bed processing of vapor product stream
US6579443B1 (en) 1998-12-07 2003-06-17 Exxonmobil Research And Engineering Company Countercurrent hydroprocessing with treatment of feedstream to remove particulates and foulant precursors
US6623621B1 (en) 1998-12-07 2003-09-23 Exxonmobil Research And Engineering Company Control of flooding in a countercurrent flow reactor by use of temperature of liquid product stream
US6822131B1 (en) 1995-10-17 2004-11-23 Exxonmobil Reasearch And Engineering Company Synthetic diesel fuel and process for its production
US6835301B1 (en) 1998-12-08 2004-12-28 Exxon Research And Engineering Company Production of low sulfur/low aromatics distillates
US20080296010A1 (en) * 2004-04-30 2008-12-04 Karl-Heinz Kirchberg Method and Device For Determining the Capacity of a Heat Exchanger
US20090288982A1 (en) * 2005-04-11 2009-11-26 Hassan Agha Process for producing low sulfur and high cetane number petroleum fuel
EP2792729A1 (en) 2013-04-17 2014-10-22 XTLgroup bv Process for hydroprocessing a liquid feed comprising hydrocarbons into fuel components

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2952626A (en) * 1957-08-05 1960-09-13 Union Oil Co Mixed-phase hydrofining of hydrocarbon oils
US3125503A (en) * 1964-03-17 Preparation of a jet fuel
US3147210A (en) * 1962-03-19 1964-09-01 Union Oil Co Two stage hydrogenation process
US3450784A (en) * 1966-09-22 1969-06-17 Lummus Co Hydrogenation of benzene to cyclohexane
US3493491A (en) * 1969-05-21 1970-02-03 Atlantic Richfield Co Blending hydrogenated fractions to make a jet fuel
US3527693A (en) * 1968-09-06 1970-09-08 Atlantic Richfield Co Process for making jet fuel
US3594307A (en) * 1969-02-14 1971-07-20 Sun Oil Co Production of high quality jet fuels by two-stage hydrogenation

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3125503A (en) * 1964-03-17 Preparation of a jet fuel
US2952626A (en) * 1957-08-05 1960-09-13 Union Oil Co Mixed-phase hydrofining of hydrocarbon oils
US3147210A (en) * 1962-03-19 1964-09-01 Union Oil Co Two stage hydrogenation process
US3450784A (en) * 1966-09-22 1969-06-17 Lummus Co Hydrogenation of benzene to cyclohexane
US3527693A (en) * 1968-09-06 1970-09-08 Atlantic Richfield Co Process for making jet fuel
US3594307A (en) * 1969-02-14 1971-07-20 Sun Oil Co Production of high quality jet fuels by two-stage hydrogenation
US3493491A (en) * 1969-05-21 1970-02-03 Atlantic Richfield Co Blending hydrogenated fractions to make a jet fuel

Cited By (29)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4102778A (en) * 1975-04-10 1978-07-25 Ruether John A Method and apparatus for carrying out hydrogenation reactions
US5183556A (en) * 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
US6274029B1 (en) 1995-10-17 2001-08-14 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US6822131B1 (en) 1995-10-17 2004-11-23 Exxonmobil Reasearch And Engineering Company Synthetic diesel fuel and process for its production
US6607568B2 (en) 1995-10-17 2003-08-19 Exxonmobil Research And Engineering Company Synthetic diesel fuel and process for its production (law3 1 1)
US6296757B1 (en) 1995-10-17 2001-10-02 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
WO1998007808A1 (en) * 1996-08-23 1998-02-26 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US5888376A (en) * 1996-08-23 1999-03-30 Exxon Research And Engineering Co. Conversion of fischer-tropsch light oil to jet fuel by countercurrent processing
US5906728A (en) * 1996-08-23 1999-05-25 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US5942197A (en) * 1996-08-23 1999-08-24 Exxon Research And Engineering Co Countercurrent reactor
AU721836B2 (en) * 1996-08-23 2000-07-13 Exxon Chemical Patents Inc. Process for increased olefin yields from heavy feedstocks
US6669743B2 (en) 1997-02-07 2003-12-30 Exxonmobil Research And Engineering Company Synthetic jet fuel and process for its production (law724)
US6309432B1 (en) 1997-02-07 2001-10-30 Exxon Research And Engineering Company Synthetic jet fuel and process for its production
US6037510A (en) * 1997-05-12 2000-03-14 Basf Aktiengesellschaft Catalytic gas-phase hydrogenation of olefins
US5882505A (en) * 1997-06-03 1999-03-16 Exxon Research And Engineering Company Conversion of fisher-tropsch waxes to lubricants by countercurrent processing
US6495029B1 (en) 1997-08-22 2002-12-17 Exxon Research And Engineering Company Countercurrent desulfurization process for refractory organosulfur heterocycles
US5928497A (en) * 1997-08-22 1999-07-27 Exxon Chemical Pateuts Inc Heteroatom removal through countercurrent sorption
US6241952B1 (en) 1997-09-26 2001-06-05 Exxon Research And Engineering Company Countercurrent reactor with interstage stripping of NH3 and H2S in gas/liquid contacting zones
US6497810B1 (en) 1998-12-07 2002-12-24 Larry L. Laccino Countercurrent hydroprocessing with feedstream quench to control temperature
US6569314B1 (en) 1998-12-07 2003-05-27 Exxonmobil Research And Engineering Company Countercurrent hydroprocessing with trickle bed processing of vapor product stream
US6579443B1 (en) 1998-12-07 2003-06-17 Exxonmobil Research And Engineering Company Countercurrent hydroprocessing with treatment of feedstream to remove particulates and foulant precursors
US6623621B1 (en) 1998-12-07 2003-09-23 Exxonmobil Research And Engineering Company Control of flooding in a countercurrent flow reactor by use of temperature of liquid product stream
US6835301B1 (en) 1998-12-08 2004-12-28 Exxon Research And Engineering Company Production of low sulfur/low aromatics distillates
US6514403B1 (en) * 2000-04-20 2003-02-04 Abb Lummus Global Inc. Hydrocracking of vacuum gas and other oils using a cocurrent/countercurrent reaction system and a post-treatment reactive distillation system
US20080296010A1 (en) * 2004-04-30 2008-12-04 Karl-Heinz Kirchberg Method and Device For Determining the Capacity of a Heat Exchanger
US7726874B2 (en) * 2004-04-30 2010-06-01 Siemens Aktiengesellschaft Method and device for determining the capacity of a heat exchanger
US20090288982A1 (en) * 2005-04-11 2009-11-26 Hassan Agha Process for producing low sulfur and high cetane number petroleum fuel
US7892418B2 (en) 2005-04-11 2011-02-22 Oil Tech SARL Process for producing low sulfur and high cetane number petroleum fuel
EP2792729A1 (en) 2013-04-17 2014-10-22 XTLgroup bv Process for hydroprocessing a liquid feed comprising hydrocarbons into fuel components

Also Published As

Publication number Publication date
IT962256B (it) 1973-12-20
FI60228B (fi) 1981-08-31
JPS5418281B2 (ja) 1979-07-06
NL7211961A (ja) 1973-03-06
NL176582C (nl) 1985-05-01
DE2242330A1 (de) 1973-03-08
FI60228C (fi) 1981-12-10
AU469396B2 (en) 1976-02-12
CA981201A (en) 1976-01-06
FR2151058B1 (ja) 1976-08-13
GB1401515A (en) 1975-07-16
FR2151058A1 (ja) 1973-04-13
ES406278A1 (es) 1975-09-16
AU4563472A (en) 1974-02-21
JPS4832903A (ja) 1973-05-04

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