US3794580A - Hydrocracking process - Google Patents
Hydrocracking process Download PDFInfo
- Publication number
- US3794580A US3794580A US00336154A US3794580DA US3794580A US 3794580 A US3794580 A US 3794580A US 00336154 A US00336154 A US 00336154A US 3794580D A US3794580D A US 3794580DA US 3794580 A US3794580 A US 3794580A
- Authority
- US
- United States
- Prior art keywords
- catalyst
- feed
- lubricating oil
- hydrocracking
- catalysts
- 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
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Classifications
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/22—Halogenating
- B01J37/26—Fluorinating
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/02—Impregnation, coating or precipitation
- B01J37/0201—Impregnation
-
- 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
- B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
- B01J37/20—Sulfiding
-
- 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
- C10G2400/10—Lubricating oil
Definitions
- the present invention relates to a process for the preparation of lubricating oil by catalytic hydrocracking of a mixture of heavy hydrocarbons.
- VI viscosity index
- this optimum catalyst is, however, applied for hydrocracking said feed to prepare a lubricating oil with a VI above the VI level for which this catalyst has been designed, a rather disappointing yield of the lubricating oil with higher VI is obtained, compared with the maximum obtainable yield of this lubricating oil from said feed.
- the optimum catalyst is applied for the preparation of a lubricating oil having the aforementioned given VI, but starting from a mixture of heavy hydrocarbons having a nitrogen and/ or aromatics content below the level for which this catalyst has been designed. Again a rather disappointing yield of the lubricating oil with the given VI is obtained, compared with the maximum obtainable yield of this lubricating oil from the feed concerned.
- An optimum catalyst for preparing a lubricating oil with a given VI by hydrocracking a mixture of heavy hydrocarbons can be applied for preparing high yields of lubracating oils having a higher VI from the same feed by adding a certain quantity of a nitrogen compound to the feed.
- the process is especially applicable for the preparation of high yields of lubricating oils having a VI greater than 100.
- addition of a nitrogen compound to the feed olferswthe possibility of preparing with a single catalyst in high yield lubricating oils having different VIs from the same feed as well as lubricating oils having the same VI from feeds having a different nitrogen and aromatics content.
- the quantity of nitrogen compound which should be added to the feed depends on the required VI level of the lubricating oil to be prepared and on the nitrogen and aromatics content of the mixture of heavy hydrocarbons which is applied as feed.
- the quantity of nitrogen compound added to the feed will be up to about 3000 p.p.m.w., with the quantity being larger as the required VI level is higher and as the nitrogen and aromatics contents of the feed is lower.
- the exact quantity of nitrogen which should be added in a certain case can easily be determined with the aid of a few scouting experiments in which different quantities of a nitrogen compound are added to the feed concerned.
- Preferred nitrogen compounds which may be added to the feed in the process according to the invention are ammonia and nitrogen compounds which yield ammonia under the conditions of the process.
- suitable nitrogen compounds are ammonia, ammonium hydroxide, alkylamines such as mono-, diand trimethylamine and mono-, diand tri-ethylamine, alkanolamines such as mono-, diand tri-ethanolamine, arylamines such as mono-, diand tri-phenylamines, mixed alkylarylamines such as phenylethylamine, alkyldiamines such as ethylenediamine and aryldiamines such as phenylenediamine.
- the higher-molecular-weight members of the various homologous series may be used as well.
- these nitrogen-containing compounds are organic nitrates, nitrites, nitriles, nitroso compounds, amides, imides, ammonium salts (such as ammonium acetate), urea and derivatives thereof, cyanates, isocyanates, isocyanides, quaternary ammonium compounds, nitro compounds, pyridine and derivatives thereof such as quinoline and piperidines, oximes, hydroxylamine and azo compounds. At least part of the quantity of nitrogen which is added to the feed may originate from ammonia which has been isolated from the hydrocracked product and recycled to the hydrocracking reactor.
- a catalyst comprising one or more metals of Groups VI-B, VII-B and/or VIII deposited on a support consisting of one or more oxides of Group II, III and/or IV elements.
- suitable metals are nickel, cobalt, molybdenum and tungsten.
- catalysts comprising at least one metal selected from the group consisting of nickel and cobalt and at least one metal selected from the group consisting of molybdenum and tungsten, inparticular catalysts comprising 0.0250.8 and more in particular ODS-0.7 gat nickel and/or cobalt and 0.050.5 and more in particular 0.1-0.4 gat molybdenum and/or tungsten per g. carrier.
- the atomic ratio between nickel and/or cobalt on the one hand and molybdenum and/0r tungsten on the other hand is preferably in the range of from 0.1:1 to 2:1 and in particular in the range of from 0.211 to 1.6:1.
- the metals may be incorporated into the catalysts by any one of the techniques for the preparation of supported catalysts well-known in the art, e.g. by coimpregnation of a carrier in one or more steps with an aqueous solution comprising salts of the metals concerned, followed by drying and calcining.
- the metals may be present on the carrier either as such or as metal oxides or metal sulphides.
- the catalysts are preferably used in their sulphidic form. Sulphidation of the catalysts may be carried out by anyone of the techniques for sulphidation of catalysts well-known in the art, e.g. by contacting the catalyst with a mixture of hydrogen and hydrogen sulphide or with hydrogen and a sulphur-containing hydrocarbon oil, such as sulphur-containing gas oil.
- Suitable carriers for the catalysts to be applied according to the present invention are silica, alumina, zirconia and magnesia, as well as mixtures of these oxides, such as silica-alumina, silica-magnesia and silica-zirconia. Preference is given to catalysts comprising as carrier material alumina or silica-zirconia.
- Catalysts employed according to the present invention may further comprise promoters such as fluorine, boron and phosphorus.
- Fluorine may be incorporated into the catalysts at any stage of the catalyst preparation. Fluorine may also be incorporated into the catalysts by in-situ fluoriding of the catalyst in an early stage (e.g. during or after start-up) of the hydrocracking process. In-situ fluoriding of the catalysts may be performed by adding a suitable fluorine compound to the gas and/ or liquid feed stream which is passed over the catalysts.
- the amount of fluorine present in the catalysts employed according to the invention is preferably 0.5 to 7 percent W.
- a catalyst which has been prepared by impregnating a porous carrier with a solution comprising (a) one or more compounds of metals selected from the group consisting of nickel, cobalt, molybdenum and tungsten, (b) phosphate ions and (c) peroxide ions, followed by drying and calcining the composite.
- a fluorine containing supported catalyst comprising at least one metal selected from the group consisting of nickel, cobalt, molybdenum and tungsten, into which catalyst at least part of the fluorine has been incorporated by fluoriding in-situ.
- a supported catalyst comprising one or more sulphides of metals selected from the group consisting of nickel, cobalt, molybdenum and tungsten which has been prepared by treating a composition comprising a porous carrier, one or more water-soluble salts of the abovementioned metals and water, with a hydrogen-sulphidecontaining gas at a temperature below 150 C. and subsequently heating up the material in a hydrogen-containing gas to a final temperature above 200 C.; the amount of water present in the composition to be treated with the hydrogen-sulphide-containing gas should correspond with the amount of water present in the composition after drying the same in a dry gas at 100 C. increased by 20 to 120% of the amount of water which said dried composition is capable of taking up within the pores of the carrier at 20 C.
- waxy lubricating oil fractions obtained in the distillation at reduced pressure of atmospheric distillation residues of waxy crude oils and waxes separated from these waxy lubricating oil fractions or from waxy lubricating oil fractions obtained by hydrocracking preference is given to waxy lubricating oil fractions obtained in the distillation at reduced pressure of atmospheric distillation residues of waxy crude oils and waxes separated from these waxy lubricating oil fractions or from waxy lubricating oil fractions obtained by hydrocracking.
- waxy lubricating oil fractions examples include spindle oil (SO), l gh machine oil (LMO) and medium hea y machine oil (MMO) waxy distillates and deasphalted oils, SO, LMO- and MMO waxy ratfinates and waxy bright stocks obtained from the above-mentioned lubricating oil fractions by treating them with a selective solvent for aromatics such as furfural, and SO, LMO, MMO-, DAO- and BS slack waxes obtained from the abovementioned lubricating oil fractions by dewaxing.
- SO spindle oil
- LMO l gh machine oil
- MMO medium hea y machine oil
- Mixtures of one or more distillate lubricating oil fractions and/or one or more residual lubricating oil fractions and/ or one or more slack waxes may also be used as starting material for the preparation of lubricating oil according to the invention.
- Very attractive results can be obtained with the following mixtures of heavy hydrocarbons as starting materials: deasphalted residual petroleum fractions and raflinates prepared from these deasphalted petroleum petroleum fractions or from heavy cat cracker cycle oils by treating them with a selected solvent for aromatics such as furfural.
- the nitrogen content of these heavy hydrocarbon fractions before addition of nitrogencontaining compounds amounts to less than 3000 p.p.m.w.
- Hydrocracking of heavy hydrocarbon fractions for the production of lubricating oil according to the invention is carried out by contacting the heavy hydrocarbon fractions, after addition of the required quantity of nitrogen thereto, at elevated temperature and pressure and in the presence of hydrogen, with a suitable catalyst, which is preferably present in one or more beds of particles of a size between 0.5 and 3 mm.
- Suitable hydrocracking conditions are: a temperature of from 350 to 450 C., a pressure of from 5 to 250 bar, a hydrogen/feed ratio of from to 5000 N 1 hydrogen per kg. feed and a space velocity of from 0.2 to 5.0 kg. feed per litre of catalyst per hour. It is preferred to apply the following conditions: a temperature of from 375 to 425 C., a pressure of from 100 to 200 bar, a hydrogen/ feed ratio of from 500 to 2500 N 1 hydrogen per kg. feed and a space velocity of from 0.5 to 1.5 per litre of catalyst per hour.
- Lubricating oils prepared by the process of the invention have a low aromatics content.
- Lubricating oils with still lower aromatics content can be prepared by the process according to the invention if the hydrocracking step is followed by a hydrofinishing step.
- Hydrofinishing of the hydrocrackate may be effected by contacting the hydrocrackate, at elevated temperature and pressure and in the presence of hydrogen, with a hydrofinishing catalyst.
- the pressure, space velocity and gas rate which are applied in the hydrofinishing step may be selected within the same ranges as given above for the hydrocracking step.
- the hydrofinishing temperature is preferably selected between 225 and 400 C. and in particular between 275 and 375 C.
- the temperature adapted in the hydrofinishing step should be at least 25 C. below the temperature at which the hydrocracking step is effected.
- Suitable hydrofinishing catalysts are catalysts comprising one or more metals of Groups VIB, VII-B and/or VIII on a carrier.
- the eflluent of the hydrocracking reactor, or, if hydrofinishing is applied, the efiiuent from the hydrofinishing reactor is cooled and separated into a hydrogen-rich gas and a liquid product.
- the liquid product contains hydrocarbons boiling below the boiling range of lubricating oil and hydrocarbons boiling within the said range.
- the hydrocarbons which boil below said range are separated from the higher-boiling residue, preferably by fractional distillation.
- the cutting point of this distillation is preferably selected such that the high-boiling residue has an initial boiling point in the range of from 350 to 550 C.
- this residue In addition to excellent lubricating oil components, this residue generally contains n-paraffins which solidify at ambient temperature and consequently have an adverse effect on the pour point of the lubricating oil. In order to produce a suitable lubricating oil from the residue it is therefore preferred to dewax this residue.
- the dewaxing treatm nt may be carried out in any manner desired.
- waxing is preferably effected by means of a mixture of methyl ethyl ketone and toluene at a temperature between and 40 C. and at a solvent-to-oil volume ratio of between 1:1 and 10: 1.
- Catalyst A Ni/Mo/P/Al- O catalyst comprising 0.06 gat nickel, 0.15 gat molybdenum and 3.1 p.b.w. phosphorus per 100 p.h.w. alumina.
- This catalyst had been prepared by impregnating alumina with an aqueous solution comprising nickel nitrate, phosphoric acid, ammonium molybdate and hydrogen peroxide followed by drying and calcining the composite.
- Catalyst B Ni/Mo/P/F/Al O catalyst containing 2.6 percent w. fluorine. This catalyst had been prepared by impregnation of catalyst A with an aqueous solution of ammonium fluoride followed by drying and calcining the composite.
- Catalyst D Ni/W/F/Al O catalyst comprising 31.0 p.b.w. nickel and 58.0 p.b.w. tungsten per 100 p.b.w. alumina and 5.7% w. fluorine.
- This catalyst had been prepared by mixing an alumina hydrogel with an aqueous solution comprising nickel nitrate, ammonium tungstate and ammonium fluoride of which solution the pH had been adjusted to 6.5 with the aid of 25% ammonia. The mixture was heated at 80 C.; the gel was filtered, extruded, dried and calcined.
- the alumina applied for the preparation of this catalyst gave on drying and calcining a xerogel having compacted bulk density between 0.75 and 1.6 g./ml. and a pore volume between 0.15 and 0.5 ml./ g.
- Catalyst E Ni/W/F/Al O' catalyst comprising 3.3 p.b.w. nickel and 25.4 p.b.w. tungsten per 100 p.b.w. alumina and 3.7 percent w. fluorine.
- This catalyst had been prepared by im pregnating alumina with an aqueous solution of am monium tungstate and nickel nitrate. After adjusting the degree of wetting to 100% the composition was first treated with H 8 at bar gauge and 75 C. for 16 hours, subsequently heated in a stream of H S-containing H (9 percent v. H 8, 10 bar gauge, 25,000 N. 1.1 .h to 400 C. within 2 hours and finally kept at 400 C. for about 2 hours in this gas stream.
- the expression degree of wetting used hereinafter refers to the amount of water which is present in the composition in addition to the amount of water present therein after drying the composition in a dry gas at 110 C.
- the degree of wetting is expressed as a percentage of the amount of water which said dried composition is capable of taking up in the pores of the carrier at C.). Fuorine had been introduced into the catalyst by in-situ fluoriding.
- Catalyst F and G Ni/W/F/Al O catalysts comprising 6.6 p.b.w. nickel and 50.8 p.b.w. tungsten per 100 p.b.w. alumina and 1.1 and 3.1 percent w. fluorine, respectively. These catalysts had been prepared in the same way as catalyst E.
- Catalyst H Ni/MofiP/F/Al O catalyst comprising 11.9 p.b.w. nickel, 20.1 p.b.w. molybdenum and 2.6 p.b.w. phosphorus per p.b.w. alumina and about 2 percent w. fluorine. Fluorine had been introduced into the catalyst by in-situ fluoriding.
- Feed IV.Raflinate obtained after extraction of Feed I with furfural. Nitrogen content: 320 p.p.m.w.; aromatic content: 47 percent w.; VI after dewaxing at 30 C.: 93.
- Feed VII.Raflinate obtained after extraction of a heavy cat. cracker cycle oil with furfural.
- Basic nitrogen content 2 p.p.m.w.
- aromatics content 27.3 mmol/ 100 g.
- 20 percent v. point in U.O.P distillation 402 C.
- the catalysts were used in the sulphided form. Sulphidation of catalysts A-D and H was carried out by contacting the catalysts with hydrogen and a sulphur-containing gas oil. Dewaxing was carried out with a 1:1 mixture of methylethyl ketone and toluene.
- Lubricating oils having a VI of 110 after topping at 400 C. and dewaxing at 30 C. were prepared by hydrocracking of Feeds I and II over catalysts B and C.
- the temperature requirements and yields of dewaxed oils are given in Table III.
- Catalysts F and G are both prepared from the same Ni/W/Al O catalyst by in-situ fluoriding and differ only in fluorine content (catalyst F: 1.1% w. F and catalyst G: 3.1% w. F).
- This experiment shows another attractive feature of the process according to the invention. If by some kind of misoperation during the in-situ fluoriding of the catalyst, too much fluorine has been incorporated therein, it is no longer necessary to replace the catalyst by one having a lower fluorine content, but it is suflicient to add a certain quantity of a nitrogen compound to the feed to be hydrocracked.
- Lubricating oils having a VI of 140 after topping at 400 C. and dewaxing at 30 C. were prepared by hydrocracking of Feeds I and III over catalyst D.
- the temperature requirements and yields of dewaxed oil are given in Table VI.
- a hydrocracking process for preparing lubricating oils having a viscosity index greater than 100 which comprises contacting a mixture of heavy hydrocarbons having a nitrogen content less than 3000 p.p.m.w. with a catalyst comprising at least one metal selected from the group consisting of nickel and cobalt and at least one metal selected from the group consisting of molybdenum and tungsten composited with a support selected from the group consisting of alumina and silica-zirconia, in the presence of hydrogen under hydrocracking conditions; and adding to said mixture of heavy hydrocarbons up to about 3000 p.p.m.w. of ammonia or a nitrogen compound which yields ammonia under the conditions of the process.
- the catalyst comprises 0.025-0.8 gram atom nickel and/or cobalt and 0.'05-0.5 gram atom molybdenum and/or tungsten per 100 grams carrier.
- hydrocracking is carried out at a temperature of from 350 to 450 C., a pressure of from 5 to 250 bar, a hydrogen/feed ratio of from to 5000 N 1 hydrogen per kg. feed and a space velocity of from 0.2 to 5.0 kg. per liter catalyst per hour.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
- Lubricants (AREA)
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GB1052272A GB1429291A (en) | 1972-03-07 | 1972-03-07 | Process for the preparation of lubricating oil |
Publications (1)
Publication Number | Publication Date |
---|---|
US3794580A true US3794580A (en) | 1974-02-26 |
Family
ID=9969383
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US00336154A Expired - Lifetime US3794580A (en) | 1972-03-07 | 1973-02-26 | Hydrocracking process |
Country Status (12)
Country | Link |
---|---|
US (1) | US3794580A (fr) |
JP (1) | JPS5918438B2 (fr) |
AU (1) | AU467628B2 (fr) |
BE (1) | BE795987A (fr) |
CA (1) | CA1011274A (fr) |
DE (1) | DE2310829A1 (fr) |
FR (1) | FR2174982B1 (fr) |
GB (1) | GB1429291A (fr) |
IT (1) | IT983493B (fr) |
NL (1) | NL7303029A (fr) |
SE (1) | SE399568B (fr) |
ZA (1) | ZA731507B (fr) |
Cited By (26)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3876522A (en) * | 1972-06-15 | 1975-04-08 | Ian D Campbell | Process for the preparation of lubricating oils |
US3915843A (en) * | 1972-12-08 | 1975-10-28 | Inst Francais Du Petrole | Hydrocracking process and catalyst for producing multigrade oil of improved quality |
US3962071A (en) * | 1973-05-19 | 1976-06-08 | Toa Nenryo Kogyo Kabushiki Kaisha | Process for producing lubricating oils |
US4428825A (en) | 1981-05-26 | 1984-01-31 | Union Oil Company Of California | Catalytic hydrodewaxing process with added ammonia in the production of lubricating oils |
US4435275A (en) | 1982-05-05 | 1984-03-06 | Mobil Oil Corporation | Hydrocracking process for aromatics production |
US4448665A (en) * | 1982-12-30 | 1984-05-15 | Exxon Research And Engineering Co. | Use of ammonia to reduce the viscosity of bottoms streams produced in hydroconversion processes |
US4469587A (en) * | 1983-09-02 | 1984-09-04 | Intevep, S.A. | Process for the conversion of asphaltenes and resins in the presence of steam, ammonia and hydrogen |
US4900707A (en) * | 1987-12-18 | 1990-02-13 | Exxon Research And Engineering Company | Method for producing a wax isomerization catalyst |
US4906601A (en) * | 1988-12-16 | 1990-03-06 | Exxon Research And Engineering Company | Small particle low fluoride content catalyst |
US4923588A (en) * | 1988-12-16 | 1990-05-08 | Exxon Research And Engineering Company | Wax isomerization using small particle low fluoride content catalysts |
US4929795A (en) * | 1987-12-18 | 1990-05-29 | Exxon Research And Engineering Company | Method for isomerizing wax to lube base oils using an isomerization catalyst |
US4937399A (en) * | 1987-12-18 | 1990-06-26 | Exxon Research And Engineering Company | Method for isomerizing wax to lube base oils using a sized isomerization catalyst |
US4959337A (en) * | 1987-12-18 | 1990-09-25 | Exxon Research And Engineering Company | Wax isomerization catalyst and method for its production |
US4992159A (en) * | 1988-12-16 | 1991-02-12 | Exxon Research And Engineering Company | Upgrading waxy distillates and raffinates by the process of hydrotreating and hydroisomerization |
US5182248A (en) * | 1991-05-10 | 1993-01-26 | Exxon Research And Engineering Company | High porosity, high surface area isomerization catalyst |
US5358628A (en) * | 1990-07-05 | 1994-10-25 | Mobil Oil Corporation | Production of high viscosity index lubricants |
US5460713A (en) * | 1992-10-02 | 1995-10-24 | Mitsubishi Oil Co., Ltd. | Process for producing low viscosity lubricating base oil having high viscosity index |
US5462650A (en) * | 1992-10-02 | 1995-10-31 | Mitsubishi Oil Co., Ltd | Process for producing low viscosity lubricating base oil having high viscosity index |
US5578197A (en) * | 1989-05-09 | 1996-11-26 | Alberta Oil Sands Technology & Research Authority | Hydrocracking process involving colloidal catalyst formed in situ |
US5643440A (en) * | 1993-02-12 | 1997-07-01 | Mobil Oil Corporation | Production of high viscosity index lubricants |
US5888377A (en) * | 1997-12-19 | 1999-03-30 | Uop Llc | Hydrocracking process startup method |
US6217747B1 (en) | 1993-07-22 | 2001-04-17 | Mobil Oil Corporation | Process for selective wax hydrocracking |
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 |
US6822131B1 (en) | 1995-10-17 | 2004-11-23 | Exxonmobil Reasearch And Engineering Company | Synthetic diesel fuel and process for its production |
EP2695675A2 (fr) | 2012-08-09 | 2014-02-12 | Eurecat Sa. | Procédé de passivation par un composé azoté d'un catalyseur zéolitique, en particulier d'un catalyseur d'hydrocraquage. |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB8425837D0 (en) * | 1984-10-12 | 1984-11-21 | Shell Int Research | Manufacture of lubricating base oils |
JPH07108984B2 (ja) * | 1985-04-01 | 1995-11-22 | 三菱化学株式会社 | 重質石炭液化物の水素化分解方法 |
US5100535A (en) * | 1987-12-03 | 1992-03-31 | Mobil Oil Corporation | Method for controlling hydrocracking operations |
US5419830A (en) * | 1985-07-26 | 1995-05-30 | Mobil Oil Corporation | Method for controlling hydrocracking and isomerization dewaxing |
JPH01185392A (ja) * | 1988-01-19 | 1989-07-24 | Nippon Oil Co Ltd | 重質石油類の水素化分解方法 |
US5098551A (en) * | 1989-05-30 | 1992-03-24 | Bertaux Jean Marie A | Process for the manufacture of lubricating base oils |
US5062943A (en) * | 1990-10-04 | 1991-11-05 | Mobil Oil Corporation | Modification of bifunctional catalyst activity in hydroprocessing |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3048536A (en) * | 1958-07-21 | 1962-08-07 | Socony Mobil Oil Co Inc | Hydrocracking process with reduction in aging of catalyst by intermittent treatment with hydrogen |
-
1972
- 1972-03-07 GB GB1052272A patent/GB1429291A/en not_active Expired
-
1973
- 1973-02-13 CA CA163,683A patent/CA1011274A/en not_active Expired
- 1973-02-26 US US00336154A patent/US3794580A/en not_active Expired - Lifetime
- 1973-02-27 BE BE1004840A patent/BE795987A/xx not_active IP Right Cessation
- 1973-03-01 IT IT21087/73A patent/IT983493B/it active
- 1973-03-05 DE DE19732310829 patent/DE2310829A1/de active Granted
- 1973-03-05 FR FR7307690A patent/FR2174982B1/fr not_active Expired
- 1973-03-05 ZA ZA731507A patent/ZA731507B/xx unknown
- 1973-03-05 NL NL7303029A patent/NL7303029A/xx not_active Application Discontinuation
- 1973-03-05 JP JP48025247A patent/JPS5918438B2/ja not_active Expired
- 1973-03-05 SE SE7303069A patent/SE399568B/xx unknown
- 1973-03-06 AU AU52965/73A patent/AU467628B2/en not_active Expired
Cited By (30)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3876522A (en) * | 1972-06-15 | 1975-04-08 | Ian D Campbell | Process for the preparation of lubricating oils |
US3915843A (en) * | 1972-12-08 | 1975-10-28 | Inst Francais Du Petrole | Hydrocracking process and catalyst for producing multigrade oil of improved quality |
US3962071A (en) * | 1973-05-19 | 1976-06-08 | Toa Nenryo Kogyo Kabushiki Kaisha | Process for producing lubricating oils |
US4428825A (en) | 1981-05-26 | 1984-01-31 | Union Oil Company Of California | Catalytic hydrodewaxing process with added ammonia in the production of lubricating oils |
US4435275A (en) | 1982-05-05 | 1984-03-06 | Mobil Oil Corporation | Hydrocracking process for aromatics production |
US4448665A (en) * | 1982-12-30 | 1984-05-15 | Exxon Research And Engineering Co. | Use of ammonia to reduce the viscosity of bottoms streams produced in hydroconversion processes |
US4469587A (en) * | 1983-09-02 | 1984-09-04 | Intevep, S.A. | Process for the conversion of asphaltenes and resins in the presence of steam, ammonia and hydrogen |
US4959337A (en) * | 1987-12-18 | 1990-09-25 | Exxon Research And Engineering Company | Wax isomerization catalyst and method for its production |
US4929795A (en) * | 1987-12-18 | 1990-05-29 | Exxon Research And Engineering Company | Method for isomerizing wax to lube base oils using an isomerization catalyst |
US4937399A (en) * | 1987-12-18 | 1990-06-26 | Exxon Research And Engineering Company | Method for isomerizing wax to lube base oils using a sized isomerization catalyst |
US4900707A (en) * | 1987-12-18 | 1990-02-13 | Exxon Research And Engineering Company | Method for producing a wax isomerization catalyst |
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EP2695675A2 (fr) | 2012-08-09 | 2014-02-12 | Eurecat Sa. | Procédé de passivation par un composé azoté d'un catalyseur zéolitique, en particulier d'un catalyseur d'hydrocraquage. |
Also Published As
Publication number | Publication date |
---|---|
SE399568B (sv) | 1978-02-20 |
FR2174982A1 (fr) | 1973-10-19 |
DE2310829C2 (fr) | 1987-07-23 |
AU467628B2 (en) | 1975-12-04 |
FR2174982B1 (fr) | 1976-04-30 |
AU5296573A (en) | 1974-09-12 |
ZA731507B (en) | 1973-12-19 |
NL7303029A (fr) | 1973-09-11 |
DE2310829A1 (de) | 1973-09-13 |
GB1429291A (en) | 1976-03-24 |
JPS48102103A (fr) | 1973-12-22 |
IT983493B (it) | 1974-10-31 |
BE795987A (nl) | 1973-08-27 |
JPS5918438B2 (ja) | 1984-04-27 |
CA1011274A (en) | 1977-05-31 |
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