US2371298A - Treatment of hydrocarbon oils - Google Patents

Treatment of hydrocarbon oils Download PDF

Info

Publication number
US2371298A
US2371298A US2371298DA US2371298A US 2371298 A US2371298 A US 2371298A US 2371298D A US2371298D A US 2371298DA US 2371298 A US2371298 A US 2371298A
Authority
US
United States
Prior art keywords
pipe
fraction
sulfur
hydrocarbons
passed
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
Publication date
Application granted granted Critical
Publication of US2371298A publication Critical patent/US2371298A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/06—Catalytic reforming characterised by the catalyst used

Definitions

  • This invention relates to the treatment of hydrocarbon oils and particularly to the treatment or etroieu'm dis'tillates.
  • This invention is particularly concerned with the treating of hydrocarbons to produce an improved motor fuel.
  • Hydrocarbon distillates, naphthas, gasoline, kerosene, and gas oils may be desulfurized in accordance with this invention.
  • the desulfurization of the hydrocarbons in the manner disclosed herein results in improved octa'ne number and lead susceptibility, characteristics which are particularly desirable in motor fuels.
  • hydrocarbonoil mixture may be treated as a whole by dehydrogenation or desulfurization to improve the quality of the oil and increase its market value.
  • Catalytic delay Sulfur impurities are effectively removed from drogenation', widely used today, improves the octane number of the hydrocarbon oil and reduces its sulfur content.
  • Catalytic desulfurization serves to remove undesirable sulfur compounds from hydrocarbons and may be carried out at much lower temperatures than those required for catalytic dehydrogenation.
  • Caustic washing and clay treating are well known means of removing undesirable impurities from the hydrocarbons.
  • the Sulfur content Ofthe etroleum distillat'es varies with the boiling point of the material.
  • the total Sulfur content in the distillates from most crudes and in most gasolines is generally higher in the higher boiling fractions than in the lower boiling fractions.
  • Hydrogen Sulfide and other very volatile sulfur compounds present in the distillates will, because of their volatility, be included in the low boiling hydrocarbons but these are readily removed by stabilization or by caustic wash and present no serious problem to the refiner.
  • Other sulfur compounds in the petroleum are usually distributed in accordance with the boiling point, being present in greater amounts in the higher boiling fractions.
  • vdi'stillathes from a given crude oil comprising the gasolines, kerosenes, naphthas, g'as oils, etc., if broken down into the different boiling range fractions Will yield low octane heavier fractions and higher octane lighter fractions.
  • All of the distlllate obtained from the topping of acrude oil may be subjected to catalytic desulfurization or catalytic dehydrogenation as known in the art.
  • Catalytic dehydrogenation using bauxite catalyst removes the sulfur impurities and improves the hydrocarbon oils by catalytic desulfurization but, aside from an improvement in the lead susceptibility, very little if any improvement is made in the octane number of the oil. While the operating conditions for catalytic desul'furization are not as severe as the operating conditions for cat alytic dehydrogenation; some damage to the octane numbers of the lighter fractions may be experienced.
  • the present'proc'ess provides a method of and apparatus for treatmentof the hydrocarbons to obtain the optimum improvement in desirable characteristics of the hydrocarbons with a minimum amount of treatment. This is accomplished by separating the distillate into fractions having different boiling ranges and treating each fraction in the manner which will result in maximum improvement in the charge stock.
  • the low oc-'- tane, high sulfur, high boiling fractions are subjected to catalytic dehydrogenation to remove the sulfur and increase their octane numbers.
  • Intermediate fractions containing sulfur are subjected to catalytic desulfurization to remove sulhydrogen; hydrogen sulfide, methane, and the like are separated from the liquid hydrocarbons.
  • the treated hydrocarbons after separation from the gas may be further treated in any conventional mannerthat may be desirable.
  • An object of this invention is to provide an improved method and apparatus for treating liydrocarbon oils.
  • Another object of this invention is to utilize waste heat contained in the eflluent of one reaction to supply the necessary heat for carrying out another reaction.
  • Still another object of this invention is to provide a process for treating a hydrocarbon mixture wherein the mixture is separated into a plurality of fractions and each fraction so treated that the maximum improvements in octane number, lead susceptibility, and sulfur content of the treated hydrocarbon mixture, result.
  • a further object of this invention is to provide novel apparatus for carrying out catalytic dehydrogenation and catalytic desulfurization.
  • FIGS 1 and 2 are diagrammatic elevation views of two specific embodiments of the present invention.
  • the numeral 4 designates a conventional fractionator.
  • the hydro carbon oil to be treated for example, a, naphtha of low octane number and high sulfur content enters the fractionator through the pipe 5, and is cut into at least three fractions of different boiling points.
  • A- fraction having an end point of about 300 F. is taken from the top of the fractionator as a vapor through the pipe 6.
  • This fraction has a relatively high octane number and contains some sulfur.
  • a higher boiling fraction, having an end point of about 450 F. is taken olf the fractionator as a liquid sidestream through the pipe 7.
  • the 450 F. end point fraction contains a higher percentage of sulfur than the overhead product and has a low octane number.
  • the remainder of the original naphtha is withdrawn from the base of the fractionator through the pipe 8, from which it may be passed to other refinery processes for further treatment.
  • the relatively high sulfur, low octane, 450 F. end point fraction is passed through the pipe I to the furnace 9 where it is vaporized and heated to a temperature in the range 900-1050 F.
  • the heated vapors are passed at this temperature and at a pressure less than 150 pounds per square inch through the pipe. l and over the bauxite catalyst in the dehydrogenator H.
  • the dehydrogenation step accomplishes reforming of some of the hydrocarbons into others of higher octane number andremoval of sulfur. A small amount of cracking may accompany the desulfurization reaction.
  • the eilluent of the dehydrogenation is passed through the pipe l2, the heat exchanger l3 and the pipe 14 to the cooler 5.
  • the relatively high octane, 300 F. end point fraction taken from the top of fractionator 4 is passed through the pipe 6 to the heat exchanger I3.
  • the temperature of this fraction is raised to the range of GOO-800 F. by indirect heat exchange with eflluent from the dehydrogenator.
  • the heated vapors pass through the pipe l6 to the desulfurizer H where it is passed over a bauxite catalyst.
  • the desulfurization is carried out at less than 150 pounds per square inch pressure and removes the sulfur withoutmhanging the structure of the hydrocarbons to any appreciable extent.
  • Efiiuent from the desulfurizer is mixed with eiiiuent from the dehydrogenator .in pipe Hi and passed to the cooler l5.
  • the cooled mixture from the cooler flows through the valve 18 and pipe [9 into the separator 20.
  • Hydrogen, hydrogen sulfide, and other gases pass off the top of the separator 20 through the pipe 2!.
  • the treated liquid hydrocarbons from the separator flow through the pipe 22 to any desirable conventional refining processes or to storage.
  • the hydrocarbons to be treated flow through the pipe 25 into the fractionator 26.
  • a low boiling, low sulfur content, high octane fraction in vapor form is passed through the pipe 27 to a condenser 28.
  • Condensate and unconclensed gases passing the condenser flow to the run tank 29.
  • the gases separated from the liquid in the run tank pass out through the valve 30 and pipe 3!.
  • Condensate is withdrawn from the run tank through the valve 32 from which it may be passed through the pipe 33 to storage or to any desirable treating process, for example, the condensate may be given a caustic wash, such processes being well known in the art and forming no part of the present invention.
  • the high boiling heavy ends are withdrawn from the base of the fractionator through the pipe 34 containing the control valve 35, to be disposed of in any suitable manner.
  • At points intermediate the top and bottom of the fractionator are drawn off fractions of different boiling ranges through the pipes 36 and 31.
  • the fraction drawn off through the pipe 31 is low octane, high sulfur, high boiling fraction suitable for dehydrogenation.
  • This fraction is passed to the furnace 33 where it is raised to dehydrogenation temperature and from which it passed through the pipe 39 to the dehydrogenator 40.
  • the dehydrogenator 40 is a catalyst chamber containing a suitable dehydrogenation catalyst. Eflluent from the dehydrogenator flows through the pipe 4
  • the fraction withdrawn from th fractionator through the pipe 36 has a good octane number and an intermediate sulfur content.
  • the boiling range is between that of the fraction drawn off through the pipe 31 and that of the fraction passing overhead through the pipe 27.
  • the fraction fiows through the pipe 36 to the desulfurizer where it is admitted through the control valve 41.:
  • a quantity of hot efiluent from the dehydrogenator, sufilcient to raise the temperature of the intermediate sulfur content fraction to the desulfurization temperature, is admitted to the desulfurizer through the control valve 45.
  • the desulfurizer 46 is a catalyst chamber filled with a suitable desulfurization catalyst. Eflluent from the desulfurizer is passed to the-cooler 43 where it is cooled and mixed with that portion of the dehydrogenation effluent passing the valve 42.
  • the method of treating hydrocarbon distillates comprising separating the hydrocarbonsinto a v contacting a high-boiling fraction with bauxite at a temperature in the range of 900-1050" F. to

Landscapes

  • 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)

Description

March 13, 1945. T. B; HUDSON ET AL' 2,371,298
TREATMENT OF HYDROCARBON OILS Filed Dec. 10, 1940 2 Sheets-Sheet 1 UOLVHVdBS INVENTOR T. B. HUDSON J. O. TURNER I BY maria a March 13, 1945. T. B. HUDSON ETAL TREATMENT OF HYDROCARBON OILS Filed Dec. 10, 1940 2 sheets-Sheet 2 HQLVHVdI-IS BOLVNHQOHQAHEIO UOLVN OI LOVELI Patented Mar. 13, 1945 UNITED STATES PATENT OFFICE TREATMENT OFiiiliZOGARBON OILS Thomas 13. Hudson and James 6. Turner, Battlesville, kla., assignors to Phillips Petroleum Company, a corporation of Delaware Application December 10, 1940, Serial No. 369;470
This invention relates to the treatment of hydrocarbon oils and particularly to the treatment or etroieu'm dis'tillates.
This invention is particularly concerned with the treating of hydrocarbons to produce an improved motor fuel. Hydrocarbon distillates, naphthas, gasoline, kerosene, and gas oils may be desulfurized in accordance with this invention. The desulfurization of the hydrocarbons in the manner disclosed herein results in improved octa'ne number and lead susceptibility, characteristics which are particularly desirable in motor fuels.
It is well known that a hydrocarbonoil mixture may be treated as a whole by dehydrogenation or desulfurization to improve the quality of the oil and increase its market value. Catalytic delay Sulfur impurities are effectively removed from drogenation', widely used today, improves the octane number of the hydrocarbon oil and reduces its sulfur content. Catalytic desulfurization serves to remove undesirable sulfur compounds from hydrocarbons and may be carried out at much lower temperatures than those required for catalytic dehydrogenation. Caustic washing and clay treating are well known means of removing undesirable impurities from the hydrocarbons.
The Sulfur content Ofthe etroleum distillat'es varies with the boiling point of the material. The total Sulfur content in the distillates from most crudes and in most gasolines is generally higher in the higher boiling fractions than in the lower boiling fractions. Hydrogen Sulfide and other very volatile sulfur compounds present in the distillateswill, because of their volatility, be included in the low boiling hydrocarbons but these are readily removed by stabilization or by caustic wash and present no serious problem to the refiner. Other sulfur compounds in the petroleum are usually distributed in accordance with the boiling point, being present in greater amounts in the higher boiling fractions.
Due to the wide variations in the crude oils from which the petroleum distillates are obtained, it is almost impossible to state rules that will be valid in every instance. Generally, however, the
vdi'stillathes from a given crude oil, comprising the gasolines, kerosenes, naphthas, g'as oils, etc., if broken down into the different boiling range fractions Will yield low octane heavier fractions and higher octane lighter fractions. All of the distlllate obtained from the topping of acrude oil may be subjected to catalytic desulfurization or catalytic dehydrogenation as known in the art. Catalytic dehydrogenation using bauxite catalyst removes the sulfur impurities and improves the hydrocarbon oils by catalytic desulfurization but, aside from an improvement in the lead susceptibility, very little if any improvement is made in the octane number of the oil. While the operating conditions for catalytic desul'furization are not as severe as the operating conditions for cat alytic dehydrogenation; some damage to the octane numbers of the lighter fractions may be experienced.
The present'proc'ess provides a method of and apparatus for treatmentof the hydrocarbons to obtain the optimum improvement in desirable characteristics of the hydrocarbons with a minimum amount of treatment. This is accomplished by separating the distillate into fractions having different boiling ranges and treating each fraction in the manner which will result in maximum improvement in the charge stock. The low oc-'- tane, high sulfur, high boiling fractions, are subjected to catalytic dehydrogenation to remove the sulfur and increase their octane numbers. Intermediate fractions containing sulfur are subjected to catalytic desulfurization to remove sulhydrogen; hydrogen sulfide, methane, and the like are separated from the liquid hydrocarbons. The treated hydrocarbons after separation from the gas may be further treated in any conventional mannerthat may be desirable.
An object of this invention is to provide an improved method and apparatus for treating liydrocarbon oils.
Another object of this invention is to utilize waste heat contained in the eflluent of one reaction to supply the necessary heat for carrying out another reaction.
Still another object of this invention is to provide a process for treating a hydrocarbon mixture wherein the mixture is separated into a plurality of fractions and each fraction so treated that the maximum improvements in octane number, lead susceptibility, and sulfur content of the treated hydrocarbon mixture, result.
A further object of this invention is to provide novel apparatus for carrying out catalytic dehydrogenation and catalytic desulfurization.
Figures 1 and 2 are diagrammatic elevation views of two specific embodiments of the present invention.
With reference to Figure 1, the numeral 4 designates a conventional fractionator. The hydro carbon oil to be treated, for example, a, naphtha of low octane number and high sulfur content enters the fractionator through the pipe 5, and is cut into at least three fractions of different boiling points. A- fraction having an end point of about 300 F. is taken from the top of the fractionator as a vapor through the pipe 6. This fraction has a relatively high octane number and contains some sulfur. A higher boiling fraction, having an end point of about 450 F. is taken olf the fractionator as a liquid sidestream through the pipe 7. The 450 F. end point fraction contains a higher percentage of sulfur than the overhead product and has a low octane number. The remainder of the original naphtha is withdrawn from the base of the fractionator through the pipe 8, from which it may be passed to other refinery processes for further treatment. The relatively high sulfur, low octane, 450 F. end point fraction, is passed through the pipe I to the furnace 9 where it is vaporized and heated to a temperature in the range 900-1050 F. The heated vapors are passed at this temperature and at a pressure less than 150 pounds per square inch through the pipe. l and over the bauxite catalyst in the dehydrogenator H. The dehydrogenation step accomplishes reforming of some of the hydrocarbons into others of higher octane number andremoval of sulfur. A small amount of cracking may accompany the desulfurization reaction. The eilluent of the dehydrogenation is passed through the pipe l2, the heat exchanger l3 and the pipe 14 to the cooler 5.
The relatively high octane, 300 F. end point fraction taken from the top of fractionator 4 is passed through the pipe 6 to the heat exchanger I3. In the heat exchanger the temperature of this fraction is raised to the range of GOO-800 F. by indirect heat exchange with eflluent from the dehydrogenator. From the heat exchanger, the heated vapors pass through the pipe l6 to the desulfurizer H where it is passed over a bauxite catalyst. The desulfurization is carried out at less than 150 pounds per square inch pressure and removes the sulfur withoutmhanging the structure of the hydrocarbons to any appreciable extent. Efiiuent from the desulfurizer is mixed with eiiiuent from the dehydrogenator .in pipe Hi and passed to the cooler l5. The cooled mixture from the cooler flows through the valve 18 and pipe [9 into the separator 20. Hydrogen, hydrogen sulfide, and other gases pass off the top of the separator 20 through the pipe 2!. The treated liquid hydrocarbons from the separator flow through the pipe 22 to any desirable conventional refining processes or to storage.
With reference to Figure 2, the hydrocarbons to be treated flow through the pipe 25 into the fractionator 26. From the top of the fractionator a low boiling, low sulfur content, high octane fraction in vapor form is passed through the pipe 27 to a condenser 28. Condensate and unconclensed gases passing the condenser flow to the run tank 29. The gases separated from the liquid in the run tank pass out through the valve 30 and pipe 3!. Condensate is withdrawn from the run tank through the valve 32 from which it may be passed through the pipe 33 to storage or to any desirable treating process, for example, the condensate may be given a caustic wash, such processes being well known in the art and forming no part of the present invention.
The high boiling heavy ends are withdrawn from the base of the fractionator through the pipe 34 containing the control valve 35, to be disposed of in any suitable manner. At points intermediate the top and bottom of the fractionator are drawn off fractions of different boiling ranges through the pipes 36 and 31. The fraction drawn off through the pipe 31 is low octane, high sulfur, high boiling fraction suitable for dehydrogenation. This fraction is passed to the furnace 33 where it is raised to dehydrogenation temperature and from which it passed through the pipe 39 to the dehydrogenator 40. The dehydrogenator 40 is a catalyst chamber containing a suitable dehydrogenation catalyst. Eflluent from the dehydrogenator flows through the pipe 4| from which it may be passed through the valve 42 to the cooler 43 or through the pipe 44 and valve 45 to the desulfurizer 46.
The fraction withdrawn from th fractionator through the pipe 36 has a good octane number and an intermediate sulfur content. The boiling range is between that of the fraction drawn off through the pipe 31 and that of the fraction passing overhead through the pipe 27. The fraction fiows through the pipe 36 to the desulfurizer where it is admitted through the control valve 41.: A quantity of hot efiluent from the dehydrogenator, sufilcient to raise the temperature of the intermediate sulfur content fraction to the desulfurization temperature, is admitted to the desulfurizer through the control valve 45. The desulfurizer 46 is a catalyst chamber filled with a suitable desulfurization catalyst. Eflluent from the desulfurizer is passed to the-cooler 43 where it is cooled and mixed with that portion of the dehydrogenation effluent passing the valve 42.
From the cooler 43 the treated hydrocarbons are passed through the pipe 48 into the separator 49. Hydrogen and other gases leave the top of the separator through the pipe 50 containing a control valve 51. Treated liquid is drawn from the separator 49 through the control valve 52 into the pipe 53 from which it may be passed to storage or further refining.
The specific embodiments described herein are given by way of illustration only and are not to be construed as limiting the present invention. While a bauxite catalyst is described, itis evident that other dehydrogenation and. desulfurization 1 catalysts, either natural or synthetic materials, may be used in the process of the present invention. The temperatures and pressures cited are those which are considered good practice at the present time for use with bauxite catalysts. If other catalysts are used, the temperatures and pressures used will be those at which the best results are obtained.
We claim:
The method of treating hydrocarbon distillates comprising separating the hydrocarbonsinto a v contacting a high-boiling fraction with bauxite at a temperature in the range of 900-1050" F. to
improve the octane number and reduce the sulfur content of the same, blending thehydrocarbon fractions, and stabilizing the treated hydrocarbons to obtain improved motor fuel.
THOMAS B. HUDSON. JAMES O. TURNER.
US2371298D Treatment of hydrocarbon oils Expired - Lifetime US2371298A (en)

Publications (1)

Publication Number Publication Date
US2371298A true US2371298A (en) 1945-03-13

Family

ID=3434481

Family Applications (1)

Application Number Title Priority Date Filing Date
US2371298D Expired - Lifetime US2371298A (en) Treatment of hydrocarbon oils

Country Status (1)

Country Link
US (1) US2371298A (en)

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2537756A (en) * 1947-11-03 1951-01-09 Porocel Corp Desulfurization of hydrocarbons
US2542970A (en) * 1946-06-15 1951-02-27 Standard Oil Dev Co Refining of cracked naphthas by selective hydrogenation
US2587987A (en) * 1949-05-10 1952-03-04 Gulf Oil Corp Selective hydrodesulfurization process
US2707700A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Gasoline refining
US2707698A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Gasoline treatment
US2707699A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Removal of thiophenes from aromatic hydrocarbons
US2717855A (en) * 1951-07-28 1955-09-13 Exxon Research Engineering Co Hydrodesulfurization of heavy oils
US2758060A (en) * 1951-01-15 1956-08-07 British Petroleum Co Removal of vanadium and/or sodium from petroleum by hydrogenation in the presence of bauxite
US2792333A (en) * 1953-04-29 1957-05-14 British Petroleum Co Catalytic hydro-reforming and hydrofining of petroleum hydrocarbons
US2892774A (en) * 1952-01-28 1959-06-30 British Petroleum Co Catalytic desulfurization of crude petroleum hydrocarbons
US2901417A (en) * 1954-05-17 1959-08-25 Exxon Research Engineering Co Hydrodesulfurization of a coked hydrocarbon stream comprising gasoline constituents and gas oil constituents
US2927891A (en) * 1955-11-16 1960-03-08 Exxon Research Engineering Co Combination heat exchange and hydrofining process
US3000810A (en) * 1957-07-03 1961-09-19 Texaco Inc Upgrading a naphtha by separation into two fractions and separate treatment of each fraction

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2542970A (en) * 1946-06-15 1951-02-27 Standard Oil Dev Co Refining of cracked naphthas by selective hydrogenation
US2537756A (en) * 1947-11-03 1951-01-09 Porocel Corp Desulfurization of hydrocarbons
US2587987A (en) * 1949-05-10 1952-03-04 Gulf Oil Corp Selective hydrodesulfurization process
US2758060A (en) * 1951-01-15 1956-08-07 British Petroleum Co Removal of vanadium and/or sodium from petroleum by hydrogenation in the presence of bauxite
US2717855A (en) * 1951-07-28 1955-09-13 Exxon Research Engineering Co Hydrodesulfurization of heavy oils
US2892774A (en) * 1952-01-28 1959-06-30 British Petroleum Co Catalytic desulfurization of crude petroleum hydrocarbons
US2707699A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Removal of thiophenes from aromatic hydrocarbons
US2707698A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Gasoline treatment
US2707700A (en) * 1952-02-19 1955-05-03 Hydrocarbon Research Inc Gasoline refining
US2792333A (en) * 1953-04-29 1957-05-14 British Petroleum Co Catalytic hydro-reforming and hydrofining of petroleum hydrocarbons
US2901417A (en) * 1954-05-17 1959-08-25 Exxon Research Engineering Co Hydrodesulfurization of a coked hydrocarbon stream comprising gasoline constituents and gas oil constituents
US2927891A (en) * 1955-11-16 1960-03-08 Exxon Research Engineering Co Combination heat exchange and hydrofining process
US3000810A (en) * 1957-07-03 1961-09-19 Texaco Inc Upgrading a naphtha by separation into two fractions and separate treatment of each fraction

Similar Documents

Publication Publication Date Title
US4062762A (en) Process for desulfurizing and blending naphtha
US2355366A (en) Process for catalytically desulphurizing hydrocarbon oil
US3364134A (en) Black oil conversion and desulfurization process
US2644785A (en) Combination crude distillation and cracking process
US2371298A (en) Treatment of hydrocarbon oils
US2763358A (en) Integrated process for the production of high quality motor fuels and heating oils
US4324935A (en) Special conditions for the hydrogenation of heavy hydrocarbons
US2419029A (en) Process for desulfurizing and reforming hydrocarbons
US2768936A (en) Conversion of asphaltic hydrocarbons
US2682496A (en) Deashing residual oils with an acid of phosphorus
US2959538A (en) Hydrodesulfurization of whole crudes
US2998381A (en) Hydrofining of middle distillate feed stock
US2901417A (en) Hydrodesulfurization of a coked hydrocarbon stream comprising gasoline constituents and gas oil constituents
US2904500A (en) Hydrogen treatment of hydrocarbons
US2167602A (en) Treatment of hydrocarbon oils
US2206921A (en) Process for desulphurization of hydrocarbons
US2398674A (en) Hydrocarbon conversion process
US2070295A (en) Treatment of hydrocarbon oils
US3758400A (en) Catalytic cracking process
US2760905A (en) Combination desulfurization and catalytic reforming process
US2761816A (en) Hydrodesulfurization process using a cobalt molybdate catalyst presulfided with the feed under specific conditions
US2906694A (en) Integrated hydrofining process
US2400795A (en) Hydrocarbon conversion process
US2891003A (en) Method of hydrodesulfurizing olefinic gasoline using an iron oxide-chromium oxide catalyst
US1944236A (en) Process for simultaneously producing high grade motor fuels and lubricants from heavy hydrocarbons by the action of hydrogen