US3077733A - Method of making jet fuel and use thereof - Google Patents

Method of making jet fuel and use thereof Download PDF

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US3077733A
US3077733A US833974A US83397459A US3077733A US 3077733 A US3077733 A US 3077733A US 833974 A US833974 A US 833974A US 83397459 A US83397459 A US 83397459A US 3077733 A US3077733 A US 3077733A
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weight percent
fuel
content
aromatic fraction
fraction extract
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William N Axe
Dean P Montgomery
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Phillips Petroleum Co
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/08—Inorganic compounds only
    • C10G21/10—Sulfur dioxide
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one extraction step
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen

Definitions

  • .tFuels produced in this manner range from about 85 per- ;cent to about 93 percent saturated. While these fuels yield certain advantages over aliphatic hydrocarbon turbojet fuels, actual tests have demonstrated that considerable difiiculties are presentwhen such fuels are utilized. In particular, coke deposits occur in the combustor chamber, the afterburner, and the tail pipe, and particularly at the combustor nozzle. The skin temperature at local- :ized regions'within the combustion chamber may become undesirably or even dangerously high. An important :contributionto such excessive temperatures is made by ;-undesirable luminosity of the flame from the fuel com- .bustion. Such luminosity causes radiation of heat to the metal and other parts of the engine.
  • a hydrodesulfurized highly .aromatic feedstock is hydrogenated to provide a and the luminosity of the flame is reduced to acceptable levels, thereby preventing the occurrence of undesirable
  • these advantages result in a substantial improvement in performance despite the fact that the hydrogenation reduces the volumetric heat content of the fuel, i.e., its density, a result considered highly undesirable by previous workers.
  • hydrodesulfurization can advantageously be accomplished with the aid of a cobalt molybdate catalyst or,
  • the highly aromatic stock can be readily hydrogenated until it is 95 percent or more saturated.
  • air is fed through an air compressor to the combustion chamber of the engine, which is formed from refractory metals or alloys designated to withstand specific combustion temperatures.
  • the resulting burned mixture is diluted with secondary air in an afterburner and expanded through a turbine which drives an air compressor. Thereupon, the gases are ejected through a jet or tail pipe into the atmosphere with
  • turboprop engines the principle of operation is essentially the same except that the majority of the energy is expended in driving the turbine which, in turn, is connected to a propeller.
  • feedstocks utilized in the process of this invention are aromatic fractions built up during the catalytic cracking of gas oil. They are derived by extraction,
  • the aromatic extract boils within the range of 450 to 1,000 F. at atmospheric pressure. It is characterized by a sulfur content of 0.25 to 2.5 weight percent, a nitrogen content of .03 to .3 Weight percent and an oxygen content of 0.25 to 2.5 weight percent.
  • the oil is at least 50 volume percent aromatic as determined by molybdate, molybdenum oxide. molybdenum sulfide, tungsten sulfide or other known hydrodesulfurization catalysts. As those skilled in the art will understand, the hydrodesulfurization is effective to remove oxygen and nitrogencontaining compounds as well as the sulfur compounds.
  • the sulfur is removed by treatment with a stoichiometric quantity of sodium (based on sodium sulfide formation) under high hydrogen pressure and elevated temperatures.
  • the quantity of hydrogen utilized in the hydrodesulfurization must be at least the stoichiometric equivalent of the quantity of sulfur, nitrogen, and oxygen present in the feed to the hydrodesulfurization step plus the quantity required to replace the sulfur, nitrogen and oxygen. To insure complete removal of these materials, the hydrogen should be at least 150 percent of the theoretical quantity required.
  • the fuel may have a final saturation of at least percent in accordance with the invention, it is essential that virtually complete removal of the sulfur, nitrogen and oxygen compounds be effected.
  • the sulfur content of the hydrodesulfurized material should be less than 0.05 percent, the nitrogen content should be below 0.05 percent, and the oxygen content should be below 0.1 percent.
  • Suitable conditions are well known to those skilled in the art and form no part of this invention. Suitable conditions are a total pressure of 1,000 pounds per square inch and a temperature of 750 F.
  • the material is then hydrogenated to provide a fuel which is 95 to percent saturated.
  • catalytic hydrogenation with a nickel, platinum or other known hydrogenation catalyst is suitable.
  • Suitable hydrogenation conditions are Well known to those skilled in the art. In general, the amount of hydrogen utilized ranges from 2500 to 5000 cubic feet per barrel hydrogenated. A pres-sure of at least 1,000 pounds per square inch or higher is suitable, and temperatures may range from 400 to 600 F.
  • the novel jet fuel composition of "the invention was made from a sulfur dioxide extract "of a cycle oil from a catalytic cracking operation.
  • Luminosity- Bureau of Mines correlation index 92 Luminosity- Bureau of Mines correlation index 92.
  • volume percent non-aromatic material 24.8.
  • This oil was solvent extracted with dimethylsulfoxide :at 180 F. and a solvent/oil ratio of 3/1.
  • the extract yield was about 75 volume'percent of the charge and had a" gravity of 2.7 API (density of 1.054 g./cc.).
  • the 'extra ct was about 5 volume percent non-aromatics.
  • the extract from the preceding step was treated by passing it twice over a cobalt molybdate catalyst which was supported on alumina.
  • the composition corresponded 'to 3 percent cobalt -oxide and 7.5 percent molybdenum oxide.
  • the treatment took place at apressure of 500 pounds per square inch, a temperature of 800 F., and a liquid hourly space velocity of 1, the amount of hydro- "gen supplied being 1,000 cubic feet per barrel of feed.
  • the material was subjected to another hydrodesulfurization treatmentntilizing a cobalt molybdate catalyst supported on alumina, the composition of which corresponded to 4.2% cobalt
  • the conditions used in this step were a temperature of 775 F., and a liquid hourly space velocity of 0.5, the amount of hydrogen supplied being 4,000 cubic feet per barrel of feed.
  • the total treatment time was 6hours. After 10 this treatment, the sulfur content was 0.05%, and the amount of oxygen and nitrogen originally present had been correspondingly reduced.
  • the product from the aforementioned hydrodesulfurization steps was fractionated, and 4.9 Weight percent ofthe material, which had a boiling point of less than 400 F., was separated from the rest of the product. About 320 parts of the material boiling above 400 F. was placed in a rocking autoclave and 74parts of a reduced nickel "on' kieselguhr hydrogenation catalyst was added.
  • Fraction 4 had an atomic ratio of carbon to hydrogen of 88.3:12.0, a net heat of combustion of 18,247 B.t.u. per pound,.a molecular weight of 263 determined by the freezing point depression method in benzene, a density of 0.9367 gram per cubic centimeter at 20 C., a viscosity ofi43centistokes at 210 C., and-a'luminometer reading of 38.5.
  • Fraction '5 had a density -of 0.9297 gram per cubic centimeter at 20C.
  • Fraction 6 had a density of 0.9683 gram per cubic'centimeter at 20 C. and a net heat of combustion of'145,200'B.t.u. per gallon.
  • the method of making a jet fuel which comprises extracting cycle oil from a catalytic cracking operation with sulfur dioxide, extracting a resulting aromatic fraction extract with dimethylsulfoxide, hydrodesulfurizing the resulting aromatic fraction extract having a sulfur content of 0.25 to 2.5 weight percent in the presence of cobalt molybdate to reduce said sulfur content to less than 0.05 weight percent, and hydrogenating the resulting material until it is 95 to 100 weight percent saturated.
  • the method of making a jet fuel which comprises extracting cycle oil from a catalytic cracking operation with a solvent selected from the group consisting of sulfur dioxide and furfural, extracting the resulting aromatic fraction extract with dimethylsulfoxide, the resulting aromatic fraction extract boiling within the range of 450 to 1000 F.
  • hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of a hydrodesulfurizing catalyst selected from the group consisting of cobalt molybdate, molybdenum oxide, molybdenum sulfide, and tungsten sulfide to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.25 weight percent and the oxygen content to below 0.1 weight percent, and hydrogenating the resulting material in the presence of a hydrogenation catalyst to provide a fuel which is 95 to 100 weight percent saturated and has a ltuninometer of at least 30.
  • a hydrodesulfurizing catalyst selected from the group consisting of cobalt molybdate, molybdenum oxide, molybdenum sulfide, and tungsten sulfide to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.25 weight percent and the oxygen content to below 0.1 weight percent, and hydrogenating the resulting material in the presence of a hydrogenation catalyst to provide a fuel which is 95 to 100
  • the method of making a jet fuel which comprises extracting cycle oil from a catalytic cracking operation with sulfur dioxide, extracting the resulting aromatic fraction extract with dimethylsulfoxide to provide an aromatic fraction extract boiling within the range of 450 to 1000 F. at atmospheric pressure and having a sulfur content of 0.25 to 2.5 weight percent, a nitrogen content of 0.03 to 0.3 weight percent and an oxygen content of 0.25 to 2.5 weight percent, hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of cobalt molybdate to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.05 weight percent and the oxygen content to below 0.1
  • hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of a hydrodesulfurizing catalyst selected from the group consisting of cobalt molybdate, molybdenum oxide, molybdenum sulfide, and tungsten sulfide to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.05 weight percent and the oxygen content to below 0.1 weight percent, and hydrogenating the resulting material in the presence of a hydrogenation catalyst to provide a fuel which is 95 to 100 weight percent saturated and has a luminometer of at least 30.

Description

- hot spots in the combustor.
3,077,733 Fatented Feb. 19, 1963 3,077,733 METHOD F MAKENG JET FUEL AND USE THEREOF William N. Axe and Dean P. Montgomery, Bartlesville,
0kla., assiguors to Phillips Petroleum Company, a corporation of Delaware No Drawing. Filed Aug. 17, 1959, Ser. No. 833,974
4 Claims. (Cl. 60-35A) desulfur-ization step, the product contains some unsaturated materials together with the saturated materials.
.tFuels produced in this manner range from about 85 per- ;cent to about 93 percent saturated. While these fuels yield certain advantages over aliphatic hydrocarbon turbojet fuels, actual tests have demonstrated that considerable difiiculties are presentwhen such fuels are utilized. In particular, coke deposits occur in the combustor chamber, the afterburner, and the tail pipe, and particularly at the combustor nozzle. The skin temperature at local- :ized regions'within the combustion chamber may become undesirably or even dangerously high. An important :contributionto such excessive temperatures is made by ;-undesirable luminosity of the flame from the fuel com- .bustion. Such luminosity causes radiation of heat to the metal and other parts of the engine.
. In accordance with this invention, a hydrodesulfurized highly .aromatic feedstock is hydrogenated to provide a and the luminosity of the flame is reduced to acceptable levels, thereby preventing the occurrence of undesirable Surprisingly, these advantages result in a substantial improvement in performance despite the fact that the hydrogenation reduces the volumetric heat content of the fuel, i.e., its density, a result considered highly undesirable by previous workers.
Where heavy cycle oil is used as a feedstock, a satura- 'tion' of 95 percent or higher cannot be attained without virtually complete removal of sulfur prior to the hydrogenation step.
The hydrodesulfurization can advantageously be accomplished with the aid of a cobalt molybdate catalyst or,
under high hydrogen pressure and elevated temperatures,
' by treatment 'witha stoichiometric quantity of sodium.
After the hydrodesulfurization treatment, the highly aromatic stock can be readily hydrogenated until it is 95 percent or more saturated.
In the operation of turbojet engines with the present fuel, air is fed through an air compressor to the combustion chamber of the engine, which is formed from refractory metals or alloys designated to withstand specific combustion temperatures.
In this chamber, the fuel and air are mixed, and the mixture is ignited.
The resulting burned mixture is diluted with secondary air in an afterburner and expanded through a turbine which drives an air compressor. Thereupon, the gases are ejected through a jet or tail pipe into the atmosphere with In turboprop engines, the principle of operation is essentially the same except that the majority of the energy is expended in driving the turbine which, in turn, is connected to a propeller.
Due to the large number of intricately shaped vanes in the turbine, it is evident that coke deposits are a very serious problem, as are such deposits in the combustion chamber or nozzle. Moreover, if the design temperature at localized regions Within the engine is exceeded, it is evident that serious damage to the engine can result, or
even a catastrophic failure.
The feedstocks utilized in the process of this invention are aromatic fractions built up during the catalytic cracking of gas oil. They are derived by extraction,
'usually with sulfur dioxide or furfural, of catalytic cracker cycle oil. The aromatic extract boils within the range of 450 to 1,000 F. at atmospheric pressure. It is characterized by a sulfur content of 0.25 to 2.5 weight percent, a nitrogen content of .03 to .3 Weight percent and an oxygen content of 0.25 to 2.5 weight percent. The oil is at least 50 volume percent aromatic as determined by molybdate, molybdenum oxide. molybdenum sulfide, tungsten sulfide or other known hydrodesulfurization catalysts. As those skilled in the art will understand, the hydrodesulfurization is effective to remove oxygen and nitrogencontaining compounds as well as the sulfur compounds. In one aspect of the invention, the sulfur is removed by treatment with a stoichiometric quantity of sodium (based on sodium sulfide formation) under high hydrogen pressure and elevated temperatures. The quantity of hydrogen utilized in the hydrodesulfurization must be at least the stoichiometric equivalent of the quantity of sulfur, nitrogen, and oxygen present in the feed to the hydrodesulfurization step plus the quantity required to replace the sulfur, nitrogen and oxygen. To insure complete removal of these materials, the hydrogen should be at least 150 percent of the theoretical quantity required.
In order that the fuel may have a final saturation of at least percent in accordance with the invention, it is essential that virtually complete removal of the sulfur, nitrogen and oxygen compounds be effected. In particular, the sulfur content of the hydrodesulfurized material should be less than 0.05 percent, the nitrogen content should be below 0.05 percent, and the oxygen content should be below 0.1 percent.
The conditions of temperature and pressure for the hydrodesulfurizationstepare well known to those skilled in the art and form no part of this invention. Suitable conditions are a total pressure of 1,000 pounds per square inch and a temperature of 750 F.
The material is then hydrogenated to provide a fuel which is 95 to percent saturated. To this end, catalytic hydrogenation with a nickel, platinum or other known hydrogenation catalyst is suitable. Suitable hydrogenation conditions are Well known to those skilled in the art. In general, the amount of hydrogen utilized ranges from 2500 to 5000 cubic feet per barrel hydrogenated. A pres-sure of at least 1,000 pounds per square inch or higher is suitable, and temperatures may range from 400 to 600 F.
AT TestFtiel-AT TetralinX 100 AT Isooctane- AT Tetralin This is not a linear measurement, and luminometer readings ofless than 30 have been found to give rise to unsatisfactory operating conditions, particularly the production of localized hot spots, in the operation of jet engines. It is surprising that'the fuel of this invention realizes the foregoing advantages and yet maintains a high net heat of combustion in-excess of 130,000 B.t.u. per gallon, the heatof vaporization of the water-of combustion being excluded fromthis figure. Moreover, the jet. fuels of the invention have low pour points below "-10" F., for example, -35 F. The density ranges between-;850 and 1.000 gram per cubic centimeter measured at 20 C.
his a feature of the invention that 'a practically quantitative removal of unsaturation can be effected by treating the hydrogenated material with silica gel. This results in'ev'en'greater advantages, particularly as regards coke disposition and production of hot spots. In particular, by'this final treatment, materials having a saturation "of 99.5 percentormore can be obtained. Instead of utilizing silica gel, the final treatment may be efiected by 'treatment'with sulfuric acid and water-washing the thus "treated material.
SPECI-FIC EXAMPLE In one' specific run, the novel jet fuel composition of "the invention was made from a sulfur dioxide extract "of a cycle oil from a catalytic cracking operation. The
oil had the following characteristics.
Luminosity- Bureau of Mines correlation index 92.
Volume percent non-aromatic material 24.8.
Two percent of the material was distilled at 518 F. an'd'95 percent of the material was distilled at 890 F. at atmospheric pressure.
' This oil was solvent extracted with dimethylsulfoxide :at 180 F. and a solvent/oil ratio of 3/1. The extract yield was about 75 volume'percent of the charge and had a" gravity of 2.7 API (density of 1.054 g./cc.). The 'extra ctwas about 5 volume percent non-aromatics.
/ The extract from the preceding step Was treated by passing it twice over a cobalt molybdate catalyst which was supported on alumina. The composition corresponded 'to 3 percent cobalt -oxide and 7.5 percent molybdenum oxide. The treatment took place at apressure of 500 pounds per square inch, a temperature of 800 F., and a liquid hourly space velocity of 1, the amount of hydro- "gen supplied being 1,000 cubic feet per barrel of feed.
'1 After this treatment, a small amount of material boiling v at less than 400 F. was separated'by fractional distillation from the remainder of the product.
Upon analysis of the product after the described hydrodesulfurization treatment, the amount of sulfur, oxygen "and nitrogen present was too high to attain the desired 5 oxide and 6.6 percent molybdenum trioxide.
extent of hydrogenauon. Accordingly, the material was subjected to another hydrodesulfurization treatmentntilizing a cobalt molybdate catalyst supported on alumina, the composition of which corresponded to 4.2% cobalt The conditions used in this step were a temperature of 775 F., and a liquid hourly space velocity of 0.5, the amount of hydrogen supplied being 4,000 cubic feet per barrel of feed. The total treatment time was 6hours. After 10 this treatment, the sulfur content was 0.05%, and the amount of oxygen and nitrogen originally present had been correspondingly reduced.
The product from the aforementioned hydrodesulfurization steps was fractionated, and 4.9 Weight percent ofthe material, which had a boiling point of less than 400 F., was separated from the rest of the product. About 320 parts of the material boiling above 400 F. was placed in a rocking autoclave and 74parts of a reduced nickel "on' kieselguhr hydrogenation catalyst was added.
ZO'Hydrog'en-Was added periodically at a temperature of I 500 Fiuntil nofurther addition of hydrogentookplace "ata total pressureof 1500 pounds. The hydrogenated product had a density of 0.909 'gram' per cubic centimeter at 2 0 C.,' a carbon -to hydrogen ratio of 87.2:13.0, a
"r'efractive index of 1.4907 at 21 C.,- and a viscosity of 50.56 -centistokes at 100 F. or 33.00 at-21'0" F. The product hada'gr'oss heat 'of c'ombustion of 148,000 B.t.u. per gallon which oorrespo'n zlsapproximately to'a net value of about 140,000. i The pour'point"was -3S--'F.
3O Thehydrogen consumption during-the hydrogenation step Fraction Bolling Point Volume V Percent Less than 400 F Y "4.5 400 to 500 F 13.8 500 to 600 F" 40.6 Over 600 F"..- 41. 1
FRACTIONS DISTILL ED FROM FRACTIONt 5 600 to 700 F -28. 8 6 Over 700 F 12.3
II- raction 3 had a net heat of cornbustion'of 137,000
' B.t.u. per gallon, a molecular Weight of 213 determined by the freezing point depression method in benzene, a --density "of-0.9037 gram per cubic-centimeter at 20 C., "a viscosity of 5.5 centistokes at 100 C., and a viscosity of 1.70 centistokes at 210 C.
Fraction 4 had an atomic ratio of carbon to hydrogen of 88.3:12.0, a net heat of combustion of 18,247 B.t.u. per pound,.a molecular weight of 263 determined by the freezing point depression method in benzene, a density of 0.9367 gram per cubic centimeter at 20 C., a viscosity ofi43centistokes at 210 C., and-a'luminometer reading of 38.5.
Fraction '5 hada density -of 0.9297 gram per cubic centimeter at 20C. Fraction 6 had a density of 0.9683 gram per cubic'centimeter at 20 C. and a net heat of combustion of'145,200'B.t.u. per gallon.
W-hen tested as a jet fuel, after a long periodof operation with fraction 3, the engine is much freer from carbon deposits than is the case wherein the engine is operated with a hydrogenated aromatic fraction whichis 92-93 percent saturated. Due to the'improved degree-of While the invention has been described inconnection with a preferred embodiment thereof, it is understood that variations in materials and conditions may be made without departing from the spirit and scope of the invention.
We claim:
1. The method of making a jet fuel, which comprises extracting cycle oil from a catalytic cracking operation with sulfur dioxide, extracting a resulting aromatic fraction extract with dimethylsulfoxide, hydrodesulfurizing the resulting aromatic fraction extract having a sulfur content of 0.25 to 2.5 weight percent in the presence of cobalt molybdate to reduce said sulfur content to less than 0.05 weight percent, and hydrogenating the resulting material until it is 95 to 100 weight percent saturated.
2. The method of making a jet fuel, which comprises extracting cycle oil from a catalytic cracking operation with a solvent selected from the group consisting of sulfur dioxide and furfural, extracting the resulting aromatic fraction extract with dimethylsulfoxide, the resulting aromatic fraction extract boiling within the range of 450 to 1000 F. at atmospheric pressure and having a sulfur content of 0.25 to 2.5 weight percent, hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of a hydrodesulfurizing catalyst selected from the group consisting of cobalt molybdate, molybdenum oxide, molybdenum sulfide, and tungsten sulfide to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.25 weight percent and the oxygen content to below 0.1 weight percent, and hydrogenating the resulting material in the presence of a hydrogenation catalyst to provide a fuel which is 95 to 100 weight percent saturated and has a ltuninometer of at least 30.
3. The method of making a jet fuel, which comprises extracting cycle oil from a catalytic cracking operation with sulfur dioxide, extracting the resulting aromatic fraction extract with dimethylsulfoxide to provide an aromatic fraction extract boiling within the range of 450 to 1000 F. at atmospheric pressure and having a sulfur content of 0.25 to 2.5 weight percent, a nitrogen content of 0.03 to 0.3 weight percent and an oxygen content of 0.25 to 2.5 weight percent, hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of cobalt molybdate to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.05 weight percent and the oxygen content to below 0.1
Weight percent, hydrogenating the resulting material in the presence of a catalyst comprising nickel to provide a hydrogenated product which is to weight percent saturated and has a luminorneter value of at least 30, treating the said hydrogenated product with a compound capable of absorbing aromatic material to provide a material which is 99 to 100 weight percent saturated, and fractionating the thus treated material to provide a fuel having a preselected boiling range for jet engine operation.
4. The method of operating a jet engine, which comprises mixing fuel and air in a combustion chamber, causing combustion of said fuel and air, and ejecting the combustion gases through a nozzle to produce a propulsive thrust, said fuel being prepared by extracting cycle oil from a catalytic cracking operation with a solvent selected from the group consisting of sulfur dioxide and furfural, extracting the resulting aromatic fraction extract with dimethylsulfoxide, the resulting aromatic fraction extract boiling within the range of 450 to 10 00" F. at atmospheric pressure and having a sulfur content of 0.25 to 2.5 weight percent, a nitrogen content of 0.03 to 0.3 weight percent, and an oxygen content of 0.25 to 2.5 weight percent, hydrodesulfurizing the latter aromatic fraction extract with hydrogen in the presence of a hydrodesulfurizing catalyst selected from the group consisting of cobalt molybdate, molybdenum oxide, molybdenum sulfide, and tungsten sulfide to reduce the sulfur content to less than 0.05 weight percent, the nitrogen content to below 0.05 weight percent and the oxygen content to below 0.1 weight percent, and hydrogenating the resulting material in the presence of a hydrogenation catalyst to provide a fuel which is 95 to 100 weight percent saturated and has a luminometer of at least 30.
References Cited in the file of this patent UNITED STATES PATENTS 1,276,219 Holmes Aug. 20, 1918 1,908,286 Dorrer May 9, 1933 2,385,981 Friedman Oct. 2, 1945 2,671,754 De Rossett et al Mar. 9, 1954 2,737,538 Nelson Mar. 6, 1956 2,768,986 Johnson et al Nov. 26, 1956 2,769,753 Hutchings et a1. Nov. 6, 1956 2,769,754 Sweetser et a1. Nov. 6, 1956

Claims (2)

1. THE METHOD OF MAKING A JET FUEL, WHICH COMPRISES EXTRACTING CYCLE OIL FROM A CATALYTIC CRACKING OPERATION WITH SULFUR DIOXIDE, EXTRACTING A RESULTING AROMATIC FRACTION EXTRACT WITH DIMETHYLSULFOXIDE, HYDRODESULFURIZING THE RESULTING AROMATIC FRACTION EXTRACT HAVING A SULFUR CONTENT OF 0.25 TO 2.5 WEIGHT PERCENT IN THE PRESENCE OF COBALT MOLYBDATE TO REDUCE SAID SULFUR CONTENT TO LESS THAN 0.05 WEIGHT PERCENT, AND HYDROGENATING THE RESULTING MATERIAL UNTIL IT IS 95 TO 100 WEIGHT PERCENT SATURATED.
4. THE METHOD OF OPERATING A JET ENGINE, WHICH COMPRISES MIXING FUEL AND AIR IN A COMBUSTION CHAMBER, CAUSING COMBUSTION OF SAID FUEL AND AIR, AND EJECTING THE COMBUSTION GASES THROUGH A NOZZLE TO PRODUCE A PROPULSIVE THRUST, SAUD FUEL BEING PREPARED BY EXTRACTING CYCLE OIL FROM A CATALYTIC CRACKING OPERATION WITH A SOLVENT SELECTED FROM THE GROUP CONSISTING OF SULFUR DIOXIDE AND FURFURAL, EXTRACTING THE RESULTING AROMATIC FRACTION EXTRACT WITH DIMETHYLSOLFOXIDE, THE RESULTING AROMATIC FRACTION EXTRACT BOILING WITHIN THE RANGE OF 450 TO 1000* F. AT ATMOSPHERIC PRESSURE AND HAVING A SULFUR CONTENT OF 0.25 TO 2.5 WEIGHT PERCENT, A NITROGEN CONTENT OF 0.03 TO 0.3 WEIGHT PERCENT, AND AN OXYGEN CONTENT OF 0.25 TO 2.5 WEIGHT PERCENT, HYDRODESULFURIZING THE LATTER AROMATIC FRACTION EXTRACT WITH HYDROGEN IN THE PRESENT, A NITROGEN CONTENT OF SULFURIZING CATALYST SELCTED FROM THE GROUP CONSISTING OF COBALT MOLYBDATE, MOLYBDENUM OXIDE, MOLYBDENUM SULFIDE, AND TUNGSTEN SULFIDE TO REDUCE THE SULFUR CONTENT TO LESS THAN 0.05 WEIGHT PERCENT AND THE OXYGEN CONTENT TO BELOW 0.05 WEIGHT PERCENT AND THE OXYGEN CONTENT TO BELOW 0.1 WEIGHT PERCENT, AND HYDROGENATING THE RESULTING MATERIAL IN THE PRESENCE OF A HYDROGENATION CATALYST TO PROVIDE A FUEL WHICH IS 95 TO 100 WEIGHT PERCENT SATURATED AND HAS A LUMINOMETER OF AT LEAST 30.
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US3175970A (en) * 1962-03-20 1965-03-30 Gulf Research Development Co Process for preparing a jet fuel
US3201345A (en) * 1962-06-14 1965-08-17 Gulf Research Development Co Process for preparing jet fuels
US3201342A (en) * 1963-01-07 1965-08-17 Exxon Research Engineering Co Method of making a superior jet fuel
US3222274A (en) * 1963-01-02 1965-12-07 Socony Mobil Oil Co Inc Process for producing high energy jet fuels
US3227768A (en) * 1962-09-20 1966-01-04 Texaco Inc Hydrogenation process
US3228993A (en) * 1962-08-23 1966-01-11 Chevron Res Catalytic hydrogenation process employing a reduced nickel- molybdenum-alumina catalyst
US3230164A (en) * 1963-06-13 1966-01-18 Shell Oil Co Hydrocracking process to produce gasoline and turbine fuels
US3313859A (en) * 1964-10-19 1967-04-11 Phillips Petroleum Co Process for hydrogenating aromatic hydrocarbons
US3367860A (en) * 1966-10-13 1968-02-06 Robert L. Barnes High density jet fuel and process for making same
US3369998A (en) * 1965-04-30 1968-02-20 Gulf Research Development Co Production of high quality jet fuels by two-stage hydrogenation
US3533938A (en) * 1967-09-06 1970-10-13 Ashland Oil Inc Jet fuel from blended conversion products
US3546098A (en) * 1968-07-24 1970-12-08 Chevron Res Making a lube oil by hydrocracking and solvent extraction
US4950820A (en) * 1985-07-24 1990-08-21 Ec Erdolchemie Gmbh Process for the hydrogenation of olefinic hydrocarbons in hydrocarbon mixtures containing tert.-alkyl alkyl ethers
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US20050059984A1 (en) * 2003-09-11 2005-03-17 Andrzej Chanduszko Devices, systems, and methods for suturing tissue
US20050192654A1 (en) * 2004-01-30 2005-09-01 Nmt Medical, Inc. Welding systems useful for closure of cardiac openings
US7666203B2 (en) 2003-11-06 2010-02-23 Nmt Medical, Inc. Transseptal puncture apparatus
US11844913B2 (en) 2012-03-23 2023-12-19 Boston Scientific Medical Device Limited Transseptal puncture apparatus and method for using the same

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Cited By (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3172833A (en) * 1965-03-09 Catalytic conversion process for the production of low luminosity fuels
US3175970A (en) * 1962-03-20 1965-03-30 Gulf Research Development Co Process for preparing a jet fuel
US3201345A (en) * 1962-06-14 1965-08-17 Gulf Research Development Co Process for preparing jet fuels
US3228993A (en) * 1962-08-23 1966-01-11 Chevron Res Catalytic hydrogenation process employing a reduced nickel- molybdenum-alumina catalyst
US3227768A (en) * 1962-09-20 1966-01-04 Texaco Inc Hydrogenation process
US3222274A (en) * 1963-01-02 1965-12-07 Socony Mobil Oil Co Inc Process for producing high energy jet fuels
US3201342A (en) * 1963-01-07 1965-08-17 Exxon Research Engineering Co Method of making a superior jet fuel
US3230164A (en) * 1963-06-13 1966-01-18 Shell Oil Co Hydrocracking process to produce gasoline and turbine fuels
US3313859A (en) * 1964-10-19 1967-04-11 Phillips Petroleum Co Process for hydrogenating aromatic hydrocarbons
US3369998A (en) * 1965-04-30 1968-02-20 Gulf Research Development Co Production of high quality jet fuels by two-stage hydrogenation
US3367860A (en) * 1966-10-13 1968-02-06 Robert L. Barnes High density jet fuel and process for making same
US3533938A (en) * 1967-09-06 1970-10-13 Ashland Oil Inc Jet fuel from blended conversion products
US3546098A (en) * 1968-07-24 1970-12-08 Chevron Res Making a lube oil by hydrocracking and solvent extraction
US4950820A (en) * 1985-07-24 1990-08-21 Ec Erdolchemie Gmbh Process for the hydrogenation of olefinic hydrocarbons in hydrocarbon mixtures containing tert.-alkyl alkyl ethers
US20040092973A1 (en) * 2002-09-23 2004-05-13 Nmt Medical, Inc. Septal puncture device
US20050059984A1 (en) * 2003-09-11 2005-03-17 Andrzej Chanduszko Devices, systems, and methods for suturing tissue
US7691112B2 (en) 2003-09-11 2010-04-06 Nmt Medical, Inc. Devices, systems, and methods for suturing tissue
US7666203B2 (en) 2003-11-06 2010-02-23 Nmt Medical, Inc. Transseptal puncture apparatus
US8992556B2 (en) 2003-11-06 2015-03-31 Pressure Products Medical Supplies, Inc. Transseptal puncture apparatus
US20050192654A1 (en) * 2004-01-30 2005-09-01 Nmt Medical, Inc. Welding systems useful for closure of cardiac openings
US7988690B2 (en) 2004-01-30 2011-08-02 W.L. Gore & Associates, Inc. Welding systems useful for closure of cardiac openings
US11844913B2 (en) 2012-03-23 2023-12-19 Boston Scientific Medical Device Limited Transseptal puncture apparatus and method for using the same

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