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US3846278A - Production of jet fuel - Google Patents

Production of jet fuel Download PDF

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Publication number
US3846278A
US3846278A US00378617A US37861773A US3846278A US 3846278 A US3846278 A US 3846278A US 00378617 A US00378617 A US 00378617A US 37861773 A US37861773 A US 37861773A US 3846278 A US3846278 A US 3846278A
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US
United States
Prior art keywords
hydrogen
feed
hydrogenation zone
hydrogenation
liquid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US00378617A
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English (en)
Inventor
M Sze
U Montclair
J Reilly
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lummus Technology LLC
Original Assignee
Lummus Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lummus Co filed Critical Lummus Co
Priority to US00378617A priority Critical patent/US3846278A/en
Priority to GB2846674A priority patent/GB1471228A/en
Priority to CA203,549A priority patent/CA1033680A/en
Priority to NL7408802A priority patent/NL7408802A/nl
Priority to DE2431436A priority patent/DE2431436A1/de
Priority to ES427884A priority patent/ES427884A2/es
Priority to FI208774A priority patent/FI60229C/fi
Priority to AU71020/74A priority patent/AU496798B2/en
Priority to JP7971774A priority patent/JPS5717911B2/ja
Priority to IT6921474A priority patent/IT1046272B/it
Priority to FR7424348A priority patent/FR2236919B2/fr
Application granted granted Critical
Publication of US3846278A publication Critical patent/US3846278A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/44—Hydrogenation of the aromatic hydrocarbons
    • C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
    • C10G45/48—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel

Definitions

  • Jet fuel is produced from a petroleum fraction boiling from about 135 F. to about 550 F., such as kerosene, by a two-stage hydrogenation process.
  • a platinum group catalyst is utilized in the first stage, a nickel catalyst in the second.
  • This invention relates to the production of jet fuel from hydrocarbon feedstocks.
  • a number of methods have been proposed for jet fuel production, from a Wide range of feedstocks.
  • various petroleum fractions or products have been subjected to hydrocracking, reforming, alkylation and other processes in various combinations.
  • U.S. Pat. 3,513,085 which discloses jet fuel production from coal liquids and petroleum oils by hydrocracking, solvent extraction, fractionation and hydrogenation is typical of such processes.
  • Other methods of producing jet fuel have involved the hydrogenation of aromatics-containing feeds in various ways, sometimes in combination with such other processes as hydrocracking.
  • 3,147,210 discloses the production of jet fuel by catalytic hydrogenation of high boiling aromatic hydrocarbons, preceded by a hydroning or hydrodesulfurization step.
  • the feedstock is desulfurized in cocurrent flow with added hydrogen in the first stage, hydrogen sulfide is stripped after the first stage; the stripped liquid is then subjected to catalytic hydrogenation in countercurrent flow with hydrogen in a second stage.
  • Application 177,362 discloses a process for production of jet fuel by a two-stage hydrogenation of a petroleumderived fraction boiling in the range of about 135 F. to about 550 F., prefereably about 300 F. to about 550 F., in which the feed is passed cocurrently with hydrogen over a hydrogenation catalyst in the first stage, and countercurrently to hydrogen over a hydrogenation catalyst, in the second stage.
  • the hydrogenation catalyst may be any of the Well-known hydrogena- 3,846,278 Patented Nov.
  • lCe tion 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, yalone or in combination.
  • Platinum group catalysts may not always result in as high a conversion rate of aromatics as may be desirable.
  • a yet further object of this invention is to provide a method for producing a jet fuel with a low aromatics content. Additionally, it is an object of this invention to provide a method for producing a jet fuel which exceeds the minimum IPT Smoke Point of 25 mm.
  • a still further object of this invention is to provide an optimum catalyst system for such a process.
  • the invention contemplates the production of jet fuel by the two-stage hydrogenation of a hydrocarbon feed having a boiling range within the temperature range of from about 135 F. to about 550 comprising the steps of: (a) passing the feed in cocurrent contact with a hydrogen-rich gas through a first hydrogenation zone operated at a temperature of from about 250 F.
  • the 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 hydrogenation catalysts 22 and 23 respectively, as discussed hereinafter.
  • the catalyst 22 in zone 16 is supported on partition 12.
  • the catalyst 23 in zone 18 is supported on a similar partition 24.
  • Partition 24 is preferably spaced somewhat above the bottom of the converter, thus dening the upper boundary of an additional lower charnber or zone 26.
  • Fresh aromatics-containing feed such as is hereinafter described, is introduced into the system at line 46, into a hydrogen stream in line 40, and the mixture proceeds in line 40 as indicated by the arrows until it joins line 44, from which may be added a condensed recycle liquid from separator 34.
  • the resulting mixture then passes through line 42 into the top of the hydrogenation vessel, at a temperature of from about 250 F. to about 575 F. and a pressure of from about 400 to about 1500 p.s.i., depending on the boiling range of the feedstock and the severity of the hydrogenation.
  • the lower temperature and pressure correspond to lower boiling feeds and lower severity of treatment.
  • the mixture of feed, recycle liquid and hydrogen passes downwardly through the catalyst bed 22 in zone 16, under adiabatic reaction conditions in which a substantial amount of the aromatics present in the total liquid charge are hydrogenated to the corresponding naphthenic cornpounds.
  • the reaction mixture which passes out of zone 16 is a two-phase mixture.
  • the liquid phase is a mixture of parains, naphthenes and some unreacted aromatics.
  • the gas phase eiuent is a mixture of hydrogen, inert gaseous impurities, and vaporized liquid hydrocarbons of a composition generally similar to that of the liquid phase euent.
  • the liquid phase of the eiuent passes downwardly through the vapor-disengaging zone 20 into the second hydrogenation zone 18 (through partition 14, which serves as a distributor plate).
  • reaction chamber 18 hydrogen introduced through line 48 passing through chamber 26 contacts the liquid phase etiluent countercurrently, hydrogenating the remaining aromatics to the corresponding naphthenes.
  • the hydrogen is introduced without being preheated, at a relatively low temperature, compared to that of the liquid phase etiluent from zone 16; generally the hydrogen temperature is no higher than about G-120 F.
  • the liquid portion which emerges from hydrogenation zone 18 is briefly accumulated in chamber 26 of the reactor, permitting disengagement of vapors and sealing the outlet to line 50 to prevent escape of hydrogen.
  • the liquid product is collected in line 50 and contains a very minor portion, generally less than 1.5 volume percent, of residual unhydrogenated aromatics.
  • the gas phase efliuent from hydrogenation zone 18 contains excess hydrogen, inert gaseous impurities, and vaporized hydrocarbons of a composition similar to those contained in the gas phase efiuent from hydrogenation zone 16.
  • the gas phase effluents from both the rst 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 is preferably cooled by being 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 30 in which it is used to preheat the mixture fed to the reactor, then 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 reliqueied 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 partially vented, as through line S6, to prevent build-up of inert impurities in the system.
  • Fresh feed hydrogen gas may be supplied from line 48 through line S8 into the recycle gas, in the event that the recycle hydrogen is insuicient to supply the needs in the rst 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 much be prevented or coke and/or 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 4S 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 vapordisengaging zone 20 and used as recycle comprise partially hydrogenated feed containing up to about 5% aromatics. Because of low concentration of aromatics, the ratio of recycle to fresh feed is less than 1:1, generally in the range of about 0.05:1 to about 0.75: 1, and depends on a number of fractors, including hydrogen partial pressure and purity, desired temperature in the reactor, aromatic content of the feed, etc.
  • nickel catalysts in a process of this type are quite sensitive to sulfur and tend to become permanently poisoned or deactivated within a relatively short time unless the feed is substantially free of sulfur (less than about 1 p.p.m.). Consequently, to utilize nickel as the catalyst in both zones of the reactor, the feed must be either naturally very low in sulfur content or must be thoroughly desulfurized before utilization. Alternatively, other catalysts may be used, but the conversion levels and residual aromatics content will not be as satisfactory.
  • a supported nickel catalyst is utilized in the second hydrogenation zone 18, with a catalyst selected from the platinum group, more specifically platinum or palladium, with platinum being preferred, being utilized in the rst hydrogenation zone 16.
  • Platinum group catalysts are only reversibly poisoned by sulfur at levels where nickel catalysts would be permanently deactivated, 'and thus, in addition to having a higher sulfur tolerance, also possess a longer catalyst life.
  • the use of the platinum group catalyst 22 in the first, or upper hydrogenation zone 16 permits the processing of feeds containing -appreciably more sulfur than if a nickel catalyst were used in -this zone.
  • feeds may be treated which contain generally up to about 5 p.p.m. sulfur, though sulfur contents as high as l p.p.m. and, in few cases, even 20 p.p.m. may be tolerated, though at these levels catalyst life may begin to decrease.
  • sulfur leaving the first hydrogenation zone 16 would be in the form of hydrogen sulfide and will be stripped out of the liquid effluent from the first zone by the hydrogen and gaseous products from the second zone 18 before coming into contact with the nickel catalyst 23.
  • catalyst bed 23 may be covered with a layer of zinc oxide which acts as a scavenger of hydrogen sulfide.
  • the platinum group catalyst is preferably supported on a support such ⁇ as alumina, silica, magnesia, zirconia or other inorganic oxides, alone or in combination or on activated charcoal.
  • a support such as ⁇ as alumina, silica, magnesia, zirconia or other inorganic oxides, alone or in combination or on activated charcoal.
  • the nickel catalyst may be supported on such materials ⁇ as various inorganic oxides, as above, diatomaceous earth or kieselguhr, alone or in combination.
  • the feed to the process comprises -a petroleum fraction having a lboiling lrange within the temperature range of from about 135 F. to about 550 F.
  • the feed can be either a straight run or other petroleum fractions; such fractions as kerosenes, light and heavy naphthas, catalytically cracked cycle oils and furnace oils can be utilized.
  • Particularly suitable is a feedstock generally boiling within the kerosene boiling range, that is, boiling within the range from about 300 F. to about 550 F.
  • the vfirst hydrogenation zone 16 is operated at a temperature of from about 300 F. -to about 575 F. and the second zone at 'about 250 F. to about 500 F., within the pressure ranges previously mentioned.
  • the process of this invention does not accomplish desulfurization forpractical purposes except to the degree mentioned previously, consequently most feedstocks should be at -least partially desu'lfurized prior to being introduced into the process, so that the sulfur content is not greater than about 20 p.p.m., preferably not gre-ater than about 10 p.p.m. and most preferably not greater than about p.p.m. This is generally performed in a separate unit (not shown).
  • the feed is desulfurized just prior to its admis-sion into the first hydrogenation zone, it will generally be sufficiently hot that no further heating is required to bring it up to reaction temperature. If, however, the feed has ⁇ been obtained from -a simple fractionation process or has been allowed to cool down prior to being passed into this process, or has been in storage, 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 preheating of the hydrogen, and feed if necessary can be accomplished in a number of ways, and can be performed separately or together.
  • a convenient method, tin this process, is to utilize the heat contained in the vapors in lines 28 .and 54 which have been removed from the vapor-disengaging zone 20.
  • the combined hydrogen (and feed, if necessary) in stream 40, together with recycle liquid from line 44, is passed through heat exchanger 30, in which it is preheated to the desired ⁇ inlet tially cooled vapors in line 54.
  • This heat exchange underv 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 34.
  • the yfresh feed is already sufficiently hot so as not to require prelieating, it should be by-passed yaround the preheater to avoid overheating and undesirable ⁇ side reactions.
  • the fresh feed will then enter the system, for example, through line 43 instead of through line 46, or the by-pass can be accomplished in other ways known in the art. 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 lbeing introduced into the reactor.
  • This separate preheating can be done using any source of -available heat, including the hot vapor mixture in line S4.
  • the ratio of hydrogen to fresh feed in the mixture fed to reaction zone 16 may vary from a stoichiometric ratio of 1 mole of hydrogen per double bond to as much as about 300% of the stoichiomertic requirement, and the ratio of hydrogen to the liquid material entering re-action 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 Iand ⁇ about 6.0, Ibased on fresh fee-d only, while that in the second zone 18 is generally at a higher level.
  • the overall L.H.S.V. is maintained, however, between 0.5 and 6.0.
  • the temperature conditions in the second zone should be adjusted to maintain the temperature of the liquid product at the outlet between about 300 and about 500 F., depending on the boiling range of the fresh feed, to provide optimum conditions favoring hydrogenation of the aromatics to naphthenes and close equilibrium approach.
  • a desulfurized straight-run kerosene having a boiling range of 350-500 F. was hydrogenated as shown in the following tabulation, illustrating the beneficial aspects of utilizing a supported nickel catalyst in the second hydrogenation zone.
  • a process for producing jet fuels by the two-stage hydrogenation of a hydrocarbon feed having a boiling range within the temperature range of about 135 F. to about 550 F. and substantially free of sulfur-containing impurities comprising the steps of:
  • step (a) comprises a member selected from the group consisting of platinum and palladium.
  • step (a) comprises platinum.
  • step (a) comprises palladium

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US00378617A 1971-09-02 1973-07-12 Production of jet fuel Expired - Lifetime US3846278A (en)

Priority Applications (11)

Application Number Priority Date Filing Date Title
US00378617A US3846278A (en) 1971-09-02 1973-07-12 Production of jet fuel
GB2846674A GB1471228A (en) 1971-09-02 1974-06-26 Production of jet fuel
CA203,549A CA1033680A (en) 1973-07-12 1974-06-27 Production of jet fuel
NL7408802A NL7408802A (nl) 1971-09-02 1974-06-28 Werkwijze voor het bereiden van straalmotor- brandstoffen.
DE2431436A DE2431436A1 (de) 1971-09-02 1974-06-29 Verfahren zur herstellung von duesentreibstoff
ES427884A ES427884A2 (es) 1973-07-12 1974-07-02 Procedimiento de obtencion de combustibles para turbinas decombustion.
FI208774A FI60229C (fi) 1973-07-12 1974-07-05 Tillverkning av braensle foer reamotor
AU71020/74A AU496798B2 (en) 1973-06-12 1974-07-09 Production of jet fuel
JP7971774A JPS5717911B2 (nl) 1973-07-12 1974-07-10
IT6921474A IT1046272B (it) 1973-07-12 1974-07-11 Procedimento per la produzione di combustibili per aviogetto da una frazione di petrolio
FR7424348A FR2236919B2 (nl) 1971-09-02 1974-07-12

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US17736271A 1971-09-02 1971-09-02
US00378617A US3846278A (en) 1971-09-02 1973-07-12 Production of jet fuel

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US3846278A true US3846278A (en) 1974-11-05

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US00378617A Expired - Lifetime US3846278A (en) 1971-09-02 1973-07-12 Production of jet fuel

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US (1) US3846278A (nl)
DE (1) DE2431436A1 (nl)
FR (1) FR2236919B2 (nl)
GB (1) GB1471228A (nl)
NL (1) NL7408802A (nl)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4208271A (en) * 1977-11-29 1980-06-17 Institut Francais Du Petrole Process for the selective hydrogenation of gasolines comprising both gum-generating compounds and undesirable sulfur compounds
US5183556A (en) * 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
JPH06507455A (ja) * 1991-11-05 1994-08-25 リーター、インゴルシュタット、シュピナライ　マシーネンバウ、アクチェンゲゼルシャフト 紡糸機紡糸単位におけるスプールの直径を確認するための方法および装置
US5522983A (en) * 1992-02-06 1996-06-04 Chevron Research And Technology Company Hydrocarbon hydroconversion process
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
EP1151060A1 (en) * 1998-12-08 2001-11-07 ExxonMobil Research and Engineering Company Production of low sulfur/low aromatics distillates
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
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
US20040238409A1 (en) * 2003-05-30 2004-12-02 Harjeet Virdi Hydrogenation of middle distillate using a counter-current reactor
US6835301B1 (en) 1998-12-08 2004-12-28 Exxon Research And Engineering Company Production of low sulfur/low aromatics distillates

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011061575A1 (en) 2009-11-20 2011-05-26 Total Raffinage Marketing Process for the production of hydrocarbon fluids having a low aromatic content
WO2011061576A1 (en) * 2009-11-20 2011-05-26 Total Raffinage Marketing Process for the production of hydrocarbon fluids having a low aromatic content
FR3015514B1 (fr) 2013-12-23 2016-10-28 Total Marketing Services Procede ameliore de desaromatisation de coupes petrolieres

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE642626A (nl) * 1963-04-11
US3369998A (en) * 1965-04-30 1968-02-20 Gulf Research Development Co Production of high quality jet fuels by two-stage hydrogenation
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

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4208271A (en) * 1977-11-29 1980-06-17 Institut Francais Du Petrole Process for the selective hydrogenation of gasolines comprising both gum-generating compounds and undesirable sulfur compounds
US5183556A (en) * 1991-03-13 1993-02-02 Abb Lummus Crest Inc. Production of diesel fuel by hydrogenation of a diesel feed
JPH06507455A (ja) * 1991-11-05 1994-08-25 リーター、インゴルシュタット、シュピナライ　マシーネンバウ、アクチェンゲゼルシャフト 紡糸機紡糸単位におけるスプールの直径を確認するための方法および装置
US5522983A (en) * 1992-02-06 1996-06-04 Chevron Research And Technology Company Hydrocarbon hydroconversion process
US6495029B1 (en) 1997-08-22 2002-12-17 Exxon Research And Engineering Company Countercurrent desulfurization process for refractory organosulfur heterocycles
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
US6569314B1 (en) 1998-12-07 2003-05-27 Exxonmobil Research And Engineering Company Countercurrent hydroprocessing with trickle bed processing of vapor product stream
US6497810B1 (en) 1998-12-07 2002-12-24 Larry L. Laccino Countercurrent hydroprocessing with feedstream quench to control temperature
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
EP1151060A1 (en) * 1998-12-08 2001-11-07 ExxonMobil Research and Engineering Company Production of low sulfur/low aromatics distillates
US6835301B1 (en) 1998-12-08 2004-12-28 Exxon Research And Engineering Company Production of low sulfur/low aromatics distillates
EP1151060A4 (en) * 1998-12-08 2010-08-18 Exxonmobil Res & Eng Co GENERATION OF DISTILLATES WITH LOW SULFUR AND FLUID CONTENT
US20040238409A1 (en) * 2003-05-30 2004-12-02 Harjeet Virdi Hydrogenation of middle distillate using a counter-current reactor
WO2004108637A2 (en) * 2003-05-30 2004-12-16 Abb Lummus Global Inc. Hydrogenation of middle distillate using a counter-current reactor
WO2004108637A3 (en) * 2003-05-30 2005-04-14 Abb Lummus Global Inc Hydrogenation of middle distillate using a counter-current reactor
US7247235B2 (en) 2003-05-30 2007-07-24 Abb Lummus Global Inc, Hydrogenation of middle distillate using a counter-current reactor

Also Published As

Publication number Publication date
NL7408802A (nl) 1975-01-14
DE2431436A1 (de) 1975-02-13
GB1471228A (en) 1977-04-21
FR2236919B2 (nl) 1978-01-20
FR2236919A2 (nl) 1975-02-07

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