US2428692A - Production of isobutane and isopentane by destructive hydrogenation of petroleum oils - Google Patents
Production of isobutane and isopentane by destructive hydrogenation of petroleum oils Download PDFInfo
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- US2428692A US2428692A US519746A US51974644A US2428692A US 2428692 A US2428692 A US 2428692A US 519746 A US519746 A US 519746A US 51974644 A US51974644 A US 51974644A US 2428692 A US2428692 A US 2428692A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
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- This invention is concerned with the production of low molecular weight hydrocarbons. More particularly, it relates to a destructive hydrogenation process employing a catalyst whereby 'large quantities oi' low molecular weight isoparaffins are'produced.
- Anobject of this invention is to provide a del structive hydrogenation process whereby large quantities of isobutane and isopentane may be obtained from a higher boiling petroleum feed stock.
- a further object of my invention is to devise a, process whereby not only are large quantities of isobutane and isopentane obtained but also high octane number aviation gasoline blending agents.
- a further object of this invention is, therefore, to provide producers of aviation gasoline with an additional process whereby further quantities of important rawmaterials employed in processes relating to the manufacture of aviation gasoline vmay be obtained.
- This process briefly comprises the destructive hydrogenation of a naphtha, ⁇ gas oil or heavier hydrocarbon in the presence of a hydrogenation catalyst possessing isomerization activity in which the unconverted heavy products are continuously recycled to ulti-- mate conversion to the desired products.
- a naphtha charge stock is destructively hydrogenated to obtain hydrocarbons of relatively low molecular weights and heavier products which may be recycled through the catalyst or a selected portion of the latter hydrocarbons may be withdrawn from the system and utilized in aviation gasoline.
- Figure 1 is a schematic drawing oi the flow plan employed in the process
- Figure 2 is a graph showing the correlation of material yields in relation to the distillate endpoint of the recycled liquidproduct.
- a hydrocarbon feed stock such as a naphtha or a gas oil having a gravity between 30-60 A. P. I. and a boiling range between about and 700 F. is passed from tank I through pipe 2 by means of pump 3 to a preheating zone 5 where it is heated to a temperature between 500 and 600 F. It is then discharged into pipe l and mixed with preheated hydrogen and heated hydrocarbons is fed by means of pipe I 0 to reactor I2 which contains a hydrogenation catalyst I4.
- the catalysts employed may comprise various metals or compounds thereof such as the sulides of nickel, cobalt, tungsten, and molybdenum, ei-
- a suit--4 able catalyst may comprise 'a mixture of nickel suliide and tungsten sulfide.
- These metal sulfldes may be impregnated 0n porous carriers or extending agents such as bauxite, acid activated clays containing bentonitic structures, synthetic or natural hydrosilicates of aluminum or magnesium, porcelain chips, charcoal, activated chars such as Nuchar, zeolites, silica gel, activated alumina and the like.
- This catalyst was prepared by treating Super Filtrol with 10% by weight of hydroiluoric acid. using a. hydroiiuoric acid'solution having an HF content of about 10% for a period of about 0.5 to 1 hour. After washing several times with water, the material was impregnated with nickel nitrate, using enough of this salt to give about 10% NizOs by weight on the catalyst. Following impregnation, the catalyst was heated to decompose the salt and the resulting oxide reduced with hydrogen.
- the hydrogenation catalyst may be any of several types which I have found to be eiective also for isomerization, as mentioned heretofore, a catalyst comprising metallic nickel deposited on HF treated ⁇ Super Filtrol is preferred.
- the conditions of hydrogenation are as follows:
- are removed through line 38 to fractionator 40.
- Light hydrocarbons',- particularly propane and small quantities of ethane, are removed as overhead through conduit 42 and may be suitably employed in other refinery processes.
- a side stream, containing hydrocarbons having 4 carbon atoms, is removed from tower 40- through pipe 46 and discharged into receiver 48. This fraction may be rectified by superfractionation in a separate distillation zone not shown in order to concentrate the isobutane present in the C4 cut.
- the bottoms from tower 40 are removed through line 50 to a secondary fractionation tower 52,from whichan overhead product is removed through line 53 which contains principally hydrocarbons having carbon atoms.
- the isopentane constituent may befurther concentrated by distillation means not shown since only conventional distillation means are required.
- the residue or bottoms from fractionator 52 may be removed through line 55 and either recycled directly to the process by 'way of pipes 55 and 62 or may alternatively be passed by way of line 56 to a third fractionating tower 58;
- this modifica- 4 centrations of isobutane and isopentane were realized by recycling materials having an initial, boiling temperature of about 160 F.
- Figure 2 it may be observed from Figure 2 that by decreasing the endpoint of the distillate from about 270 F. to 158 F., an increase in total C4 production resulted from 33 to 65 volume per- ⁇ Fresh hydrogen is withdrawn from'storage holdcent based on fresh feed.
- Substantial amounts o n-butane and n-pentane are formed in my process and these may advantageously be used as feed stocks to an isomerization process wherein further increments of the corresponding iso compounds can be obtion, the function of tower 58 is to effect a separation between hydrocarbons boiling preferably below about 160 F. and heavier materials boiling above 160 F.
- the naphtha boiling up to about 160 F. is removed overhead through line 60 and passed into run-down tank 10, since I have found that this material is an excellent blending stock for preparing aviation gasolines of superior characteristics.
- the higher boiling hydrocarbon material is removed as bottoms by way of pipe 64 and recycled to the hydrogenation process for ultimate conversion to lighter hydrocarbons.
- a stock obtained by hydrogenating Quiriquire crude oil to obtain a Cycle stock having a gravity of 44.3/A.P. I., an initial boiling point of 293 F., and a final boiling point of 469 F. was .destructively hydrogenated under the following conditions:
- my invention in its preferred application comprises destructively hydrogenating a naphtha. or light gas oil of suitably low sulfur content, preferably having a'boiling point above about F. and below about 800 F. with a catalyst comprising metallic nickel deposited on an activated clay base. Selected frac- .tions of the product are obtained by fractional distillation procedures and, of these, I have found that high concentrations of isoparaillns are pres ⁇ ent in the butane and pentane cuts.
- the isoparamns produced have a molecular weight below about 115.
- the total product boiling above pentane may advantageously be recycled to ultimate conversion for the production of maximum amounts of the desired isoparalns or else the ceding speciflcation and examples given, al
- the method of producing isobutane and isopentane which comprises destructively hydrogenating petroleum hydrocarbonsl boiling abovey about 100 F. and below about 800 F., in the presence of hydrogen and of a catalyst containing an element selected from the class consisting of nickel, cobalt, tungsten and molybdenum having hydrogenatlng and isomerizing properties, removing the isobutane and isopentane, recycling hydrocarbons having a boiling range between about 160 F. and about 225 F. and continuing .such recycling to obtain a maximum yield of isobutane and isopentane.
- fractions respectively rich in isobutane, isopentane and hydrocarbons boiling up to about 160 F. and continuously recycling said fraction having a'boiling range between about 160 F. and 225 F. for maximum conversion to isoparafiins.
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Description
7, 94?. A. VOORIES, J 2,4233@ TANE BY DESTRUCTIVE HYDROGENTION OF PETROLEUM OILS PRODUCTION 0F ISOBUTANE AND ISOPEN Filed Jan. 25, 1944 2 Sheets-51u99@1 l une@ Clvborneq PRODUCTION 0F ISOBUTANE AND ISOPENTANE BY DESTRUGTIVE HYDROGENATION OF PETROLEUM OILS Filed Jan. 26, 1944 2 Sheets-Sheet 2 lsobuwma ssamm-MNE, @Y
Daavmucfwv. HYDmOE-NAWQN es Qumnawsa Mwsaecwcges'mcm if. 0a so W ks 34o )fr g o g J laoool ged @aug 15o vrs abo zes 'afso 'z'sA J i? T, E947. A. wooRHlEs, .JR 2,428,692
'Patentedocb 719417- UNITED STATES y2,428,692 i C E PRODUCTION F ISOBUTANE AND ISOPEN- TANE I BY DESTRUCTIVE HYDROGENA- TIOIN- OF PETROLEUM OILS Alexis Voorhies, Jr., BatonRouge, La., assigner to Standard Oil Development Company, a
ration of Delaware corpo- Appilcation January 26, 1944, Serial No. 519,746
s claims. 1
This invention is concerned with the production of low molecular weight hydrocarbons. More particularly, it relates to a destructive hydrogenation process employing a catalyst whereby 'large quantities oi' low molecular weight isoparaffins are'produced.
Anobject of this invention is to provide a del structive hydrogenation process whereby large quantities of isobutane and isopentane may be obtained from a higher boiling petroleum feed stock.
A further object of my invention is to devise a, process whereby not only are large quantities of isobutane and isopentane obtained but also high octane number aviation gasoline blending agents.
Recent technical advances in the art of producing high octane number gasoline have made creased demand for aviation gasoline, it'is be' coming more difiicult for refiners to obtain adequate supplies of these valuable hydrocarbons.
A further object of this invention is, therefore, to provide producers of aviation gasoline with an additional process whereby further quantities of important rawmaterials employed in processes relating to the manufacture of aviation gasoline vmay be obtained.
I have now, developed a process whereby pre' dominant amounts of isobutane and isopentane can be produced from petroleum sources.
in rather small quantities. This process briefly comprises the destructive hydrogenation of a naphtha, `gas oil or heavier hydrocarbon in the presence of a hydrogenation catalyst possessing isomerization activity in which the unconverted heavy products are continuously recycled to ulti-- mate conversion to the desired products.
In one variation of my process, a naphtha charge stock is destructively hydrogenated to obtain hydrocarbons of relatively low molecular weights and heavier products which may be recycled through the catalyst or a selected portion of the latter hydrocarbons may be withdrawn from the system and utilized in aviation gasoline.
Otherlight gases are also obtained, but these are found Further objects of the invention will be ap' parent from the following specification when considered together with the accompanying drawings in which:
Figure 1 is a schematic drawing oi the flow plan employed in the process;
Figure 2 is a graph showing the correlation of material yields in relation to the distillate endpoint of the recycled liquidproduct.
As shown in Figure l, a hydrocarbon feed stock such as a naphtha or a gas oil having a gravity between 30-60 A. P. I. and a boiling range between about and 700 F. is passed from tank I through pipe 2 by means of pump 3 to a preheating zone 5 where it is heated to a temperature between 500 and 600 F. It is then discharged into pipe l and mixed with preheated hydrogen and heated hydrocarbons is fed by means of pipe I 0 to reactor I2 which contains a hydrogenation catalyst I4.
The catalysts employed may comprise various metals or compounds thereof such as the sulides of nickel, cobalt, tungsten, and molybdenum, ei-
ther alone or in admixture. For example, a suit--4 able catalyst may comprise 'a mixture of nickel suliide and tungsten sulfide. These metal sulfldes may be impregnated 0n porous carriers or extending agents such as bauxite, acid activated clays containing bentonitic structures, synthetic or natural hydrosilicates of aluminum or magnesium, porcelain chips, charcoal, activated chars such as Nuchar, zeolites, silica gel, activated alumina and the like. I have preferred, however, to employ a catalyst comprising metallic nickel de-v posited on acid-activated clay vsincefunexpectedly higher yields of isoparafllns.4 are obtained with this catalyst than with. themetal sulfide types.
This catalyst was prepared by treating Super Filtrol with 10% by weight of hydroiluoric acid. using a. hydroiiuoric acid'solution having an HF content of about 10% for a period of about 0.5 to 1 hour. After washing several times with water, the material was impregnated with nickel nitrate, using enough of this salt to give about 10% NizOs by weight on the catalyst. Following impregnation, the catalyst was heated to decompose the salt and the resulting oxide reduced with hydrogen.
While it is obvious that the hydrogenation catalyst may be any of several types which I have found to be eiective also for isomerization, as mentioned heretofore, a catalyst comprising metallic nickel deposited on HF treated `Super Filtrol is preferred. The conditions of hydrogenation are as follows:
Hydrogen recycle rate, CF/B 2---- 5,000 to 10,000
1 Volume of liquid feed er volume of catal st er hour. 2 Cubic feet per barrellif feed. y p
The products ofl hydrogenation are removed overhead from reactor I2 through line I6, passed through cooler" I8v and line I9 to high pressure separator 2 I. Light gases consistingA of hydrogen and low molecular weight hydrocarbons such as methane, ethane and propane are removed overhead from separator 2| byy way of pipe 22 and pump 24 and recycled to the system, although a portion thereof may be vented through pipe 30.
er 28 through line 23 and pump 32', mixed with recycle hydrogen, preheated in furnace 34 to a temperature below that maintained in the reactor I2 and discharged by means of pipe 36 into pipe l where it is mixed with the preheated hydrocarbon feed, and is then passed through the reaction zone.
The liquid hydrocarbon products which are separated in separator 2| are removed through line 38 to fractionator 40. Light hydrocarbons',- particularly propane and small quantities of ethane, are removed as overhead through conduit 42 and may be suitably employed in other refinery processes. A side stream, containing hydrocarbons having 4 carbon atoms, is removed from tower 40- through pipe 46 and discharged into receiver 48. This fraction may be rectified by superfractionation in a separate distillation zone not shown in order to concentrate the isobutane present in the C4 cut. The bottoms from tower 40 are removed through line 50 to a secondary fractionation tower 52,from whichan overhead product is removed through line 53 which contains principally hydrocarbons having carbon atoms. If desired, the isopentane constituent may befurther concentrated by distillation means not shown since only conventional distillation means are required. The residue or bottoms from fractionator 52 may be removed through line 55 and either recycled directly to the process by 'way of pipes 55 and 62 or may alternatively be passed by way of line 56 to a third fractionating tower 58; In this modifica- 4 centrations of isobutane and isopentane were realized by recycling materials having an initial, boiling temperature of about 160 F. For example, it may be observed from Figure 2 that by decreasing the endpoint of the distillate from about 270 F. to 158 F., an increase in total C4 production resulted from 33 to 65 volume per- `Fresh hydrogen is withdrawn from'storage holdcent based on fresh feed. Likewise, the total Cs produced increasedfrom about 23 to about 43% by volume on fresh feed. It will be noticed that the proportion of isobutane to n-butane remained approximately constant. As previously stated, the liquid yield'of isobutane, calculated as volume percent on the fresh feed,was 52.2% when the distillate had an endpoint of 158 F., and under these same conditions the isopentane production amounted to 38%. This high production of isopentane I consider to be important since isopentane is utilized as a blending agent in gasoline of high octane number rating and not only provides volatility but also contributes to the high octane quality of the gasoline.
Substantial amounts o n-butane and n-pentane are formed in my process and these may advantageously be used as feed stocks to an isomerization process wherein further increments of the corresponding iso compounds can be obtion, the function of tower 58 is to effect a separation between hydrocarbons boiling preferably below about 160 F. and heavier materials boiling above 160 F. The naphtha boiling up to about 160 F. is removed overhead through line 60 and passed into run-down tank 10, since I have found that this material is an excellent blending stock for preparing aviation gasolines of superior characteristics. The higher boiling hydrocarbon material is removed as bottoms by way of pipe 64 and recycled to the hydrogenation process for ultimate conversion to lighter hydrocarbons.
In a specific example, a stock obtained by hydrogenating Quiriquire crude oil to obtain a Cycle stock having a gravity of 44.3/A.P. I., an initial boiling point of 293 F., and a final boiling point of 469 F. was .destructively hydrogenated under the following conditions:
Average temperature, F 700 Feed rate, v./v./hr 1.0 Recycle gas rate, CF/B 8,000 Pressure, p.'s. i. g 3,000
Under these conditions, when recycling all material boiling above 158 F., 38.1 volume percent of isopentane on fresh feed and 52.2 volume percent of isobutane on fresh feed were obtained, along with 218 cubic feet of propane 'per barrel of fresh feed. As a result of detailed experiments, I have also found that it is possible to obtain high total yields of isobutane and isopentane by recycling hydrocarbons boiling up to about 225 F.
As maybe seen from Figure 2, much higher cont'ained.
While I may recycle the total liquid product removed vas bottom from fractionator 52 through lines 55 and 62, I prefer, however, to recycle only the heavier portions thereof boiling above about 160 F. It is also obvious that, should the supply of feed stock become limited, I would prefer to recycle all of the liquid material in order to obtain the maximum quantity of iso-C4 and iso-Cs hydrocarbons. In addition to these products, I have found that smaller quantities of ethane and propane are formed and these may be used for fuel purposes. In the case of propane. however, it may be subjected to a pyrolytic conversion treatment for the production of propylene and ethylene which may then be employed in y alkylation processes.
I ha've determined that the A. S. T, M. octane number of the pentane-Iree distillate, having an endpoint of 158 F., produced in my process is j 81.1 clear and, with 3 cc. lead tetraethyl per gallon added, is 97.5. Likewise, I have found that the A. S. T. M. octane number of a pentane-free distillate having an endpoint of 1967 F. is 78.5 clear, and 94.2 with 3 cc. lead tetraethyl added. The A. S. T. M. octane number of a pentane-fjree distillate having an endpoint of 275 F. is only 75.5 clear, and 89.4 when containing 3 cc. of lead tetraethyl per gallon. It'will be noted that, as the endpoint of the distillate increases, the octane number'decreases and in one modication of my invention, I propose to limit the endpoint of the naphtha which I desire tov include in aviation gasolines to about 160 F.
To recapitulate, I have devised an eflicient process for producing significant quantities of low molecular weight isoparailins, particularly isobutane andisopentane, as well as hydrocarbon components suitable for blending in aviation gasolines. Substantially, my invention in its preferred application comprises destructively hydrogenating a naphtha. or light gas oil of suitably low sulfur content, preferably having a'boiling point above about F. and below about 800 F. with a catalyst comprising metallic nickel deposited on an activated clay base. Selected frac- .tions of the product are obtained by fractional distillation procedures and, of these, I have found that high concentrations of isoparaillns are pres` ent in the butane and pentane cuts. Preferably the isoparamns produced have a molecular weight below about 115. In addition, I have found that the total product boiling above pentane may advantageously be recycled to ultimate conversion for the production of maximum amounts of the desired isoparalns or else the ceding speciflcation and examples given, al
though neither section is intended to limit unduly its general broad scope.
I claim as my invention:
1. The method of producing isobutane and isopentane, which comprises destructively hydrogenating petroleum hydrocarbonsl boiling abovey about 100 F. and below about 800 F., in the presence of hydrogen and of a catalyst containing an element selected from the class consisting of nickel, cobalt, tungsten and molybdenum having hydrogenatlng and isomerizing properties, removing the isobutane and isopentane, recycling hydrocarbons having a boiling range between about 160 F. and about 225 F. and continuing .such recycling to obtain a maximum yield of isobutane and isopentane.
2. The method, according to claim 1in which the catalyst comprises metallic nickel supported on an acid-activated clay.
3. The method. according to claim 1, in which the catalyst comprises metallic nickel supported on a clay base which has been activated by successive treatments with sulfuric acid and hydrofiuoric acid.
4. The method of producing isobutane and iso-- pentane, which comprises destructively hydrogenating a normally liquid petroleum distillate oil in the presence oi hydrogen and of a catalyst comprising nickel ,supported on acid activated clay, at a temperature between'-about 600 and 800 F., and a pressure of about`1',000 to 5,000 pounds per square inch, employing a feed rate between 0.5 and 5.0 `liquid-=volumes per volume of catalyst per hour. recycling hydrocarbons boiling in the range of about 160 F. to 225 F.. and' continuing such recycling to obtain a maximum yield of isobutane and isopentane.
5. In a process for the production of isoparafflns having a molecular weight below about 115. which comprises destructively hydrogenating normally liquid petroleum distillates at elevated temperatures and pressures in the presence of hydrogen in a reaction zone containing a supported hydrogenatlon catalyst containing an element selected from the-class consisting of nickel, cobalt, tungsten and molybdenum, withdrawing casacca the reaction productsfrom the reaction zone, segregating the reaction products into a series of separate streams of consecutively higher boiling range, each of which said streams contains a substantial quantity of isoparafllnic constituents, and a higher boiling liquid fraction, the step of fractionating to obtain a higher boiling liquid fraction having a boiling range of about 160 F. to 225 F., and continuouslyrecycling said fraction to the reaction zone for maximum conversion to isoparailins.
6. In a process for the production of low molecular weight isoparaill-ns -comprlsing passing a normally liquid petroleum distillate in the presence of hydrogen through a zone charged with a supported metallic hydrogenation catalyst containing an element selected from the class consisting of nickel, cobalt, tungsten and molybdenum and maintained under destructive-heydrogenation conditions of pressure and temperature, removing the reaction products from the reaction zone and discharging them into a distillation zone, and fractionating the products thereof, the steps of separating a fraction rich in lsobutane, a fraction rich in isopentane, a fraction boiling up to about 160 E., and a fraction having a boiling range between about 160 F. and 225 removing from the process. the fractions respectively rich in isobutane, isopentane and hydrocarbons boiling up to about 160 F., and continuously recycling said fraction having a'boiling range between about 160 F. and 225 F. for maximum conversion to isoparafiins.
ALEXIS VOORI-IIES, JR.
REFERENCES CITED The following references are of record in the ille of this patent:
UNITED STATES PATENTS Number Name Date 2,319,495 Egloff May 18, 1943 2,324,762 Calhoun et al. July 20, 1943 2,337,418 Ruthrufl Dec. 21, 1943 2,232,909 'Gohr Feb. 25, 1941 2,326,627 Eglolt` et al Aug. 10, 1943 2,290,189 Ipatiefl' et al. July 21, 1942 2,334,553 Harding Nov. 16, 1943 2,344,789 Schmerling Mar, 21, 1944 2,357,495 Bloch Sept. 5, 1944 2,366,699 Crockett et al Jan. 9. 1945 FOREIGN PATENTS Number Country 4Date 527,767 Great Britain Oct. 16, 1940 550,480 Great Britain Jan. 11, 1943 OTHER REFERENCES
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US519746A US2428692A (en) | 1944-01-26 | 1944-01-26 | Production of isobutane and isopentane by destructive hydrogenation of petroleum oils |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US519746A US2428692A (en) | 1944-01-26 | 1944-01-26 | Production of isobutane and isopentane by destructive hydrogenation of petroleum oils |
| GB2064744A GB587048A (en) | 1944-10-24 | 1944-10-24 | Improved process for the destructive hydrogenation of petroleum hydrocarbons |
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| US2428692A true US2428692A (en) | 1947-10-07 |
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| US519746A Expired - Lifetime US2428692A (en) | 1944-01-26 | 1944-01-26 | Production of isobutane and isopentane by destructive hydrogenation of petroleum oils |
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Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2709151A (en) * | 1950-12-01 | 1955-05-24 | Basf Ag | Process for the recovery of gasoline from petroleum oils or crude residues by destructive hydrogenation with the use of a catalyst |
| US2915571A (en) * | 1957-11-13 | 1959-12-01 | Universal Oil Prod Co | Isomerization of saturated hydrocarbons |
| US2946738A (en) * | 1957-07-01 | 1960-07-26 | Phillips Petroleum Co | Hydrocracking a gas oil with a presulfided catalyst consisting of oxides of vanadium, cobalt and molybdenum on gamma alumina |
| US2970954A (en) * | 1958-02-14 | 1961-02-07 | Socony Mobil Oil Co Inc | Selective demethylation of hydrocarbon mixtures containing saturated and unsaturated hydrocarbons |
| US3044953A (en) * | 1959-03-30 | 1962-07-17 | California Research Corp | Removal of an undecane-rich fraction from a hydrocarbon conversion process recycle |
| US3047490A (en) * | 1958-11-04 | 1962-07-31 | Phillips Petroleum Co | Hydrocracking process |
| US3110662A (en) * | 1960-06-24 | 1963-11-12 | California Research Corp | Catalytic conversion process for the production of low freezing point fuels |
| US3128243A (en) * | 1960-06-29 | 1964-04-07 | California Research Corp | Hydrocracking process with an aluminanickel sulfide catalyst activated with bf3 |
| US3130240A (en) * | 1961-11-16 | 1964-04-21 | Phillips Petroleum Co | Process for the activation of hydrogenation catalysts |
| US3135682A (en) * | 1961-01-03 | 1964-06-02 | California Research Corp | Process for producing gasoline from a cracked feed stock by catalytic hydrocracking |
| US3153100A (en) * | 1960-06-28 | 1964-10-13 | California Research Corp | Process for converting monoalkyl-substituted monocyclic naphthenes |
| US3153627A (en) * | 1960-04-04 | 1964-10-20 | Gulf Research Development Co | Catalytic process |
| US3172834A (en) * | 1965-03-09 | Process for manufacturing gasoline by blending the hydrocracked gasoline with the dehydrogenated and alkyl- ated products obtained from the hy- drocracking stage | ||
| US3180818A (en) * | 1962-12-03 | 1965-04-27 | California Research Corp | Two stage hydrocarbon conversion process with hydrocracking in both stages to produce a high octane gasoline |
| US3209052A (en) * | 1963-01-17 | 1965-09-28 | Shell Oil Co | Integrated hydration-isomerization process |
| US3242067A (en) * | 1961-10-31 | 1966-03-22 | Exxon Research Engineering Co | Fluid hydrogenative cracking process with the use of unsulfided metallic nickel on a cracking catalyst support |
| US3303124A (en) * | 1964-12-24 | 1967-02-07 | Shell Oil Co | Catalytic hydrocracking of naphthas with the use of a catalyst composite comprising copper on a siliceous support |
| US3385782A (en) * | 1966-05-06 | 1968-05-28 | Chevron Res | Production of light hydrocarbon gases by hydrocracking high boiling hydrocarbons |
| US3432568A (en) * | 1966-06-20 | 1969-03-11 | Mobil Oil Corp | Upgrading of hydrocarbons in the presence of a mixed alumino-silicate and metal catalyst |
| US3530060A (en) * | 1968-12-30 | 1970-09-22 | Mobil Oil Corp | Gasoline manufacture |
| US4101592A (en) * | 1977-02-04 | 1978-07-18 | Phillips Petroleum Company | Catalytic hydrogenation |
| US5246567A (en) * | 1992-02-10 | 1993-09-21 | Amoco Corporation | Benzene removal in an isomerization process |
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| GB527767A (en) * | 1938-03-15 | 1940-10-16 | Ig Farbenindustrie Ag | Improvements in the isomerisation of low molecular paraffinic hydrocarbons |
| US2232909A (en) * | 1939-06-20 | 1941-02-25 | Standard Ig Co | Hydrogenation process |
| US2337418A (en) * | 1939-11-15 | 1943-12-21 | Robert F Ruthruff | Destructive isomerization |
| US2290189A (en) * | 1939-12-13 | 1942-07-21 | Universal Oil Prod Co | Conversion of straight chain olefins to isoparaffins |
| US2319495A (en) * | 1940-04-22 | 1943-05-18 | Universal Oil Prod Co | Treatment of hydrocarbons |
| US2326627A (en) * | 1940-09-30 | 1943-08-10 | Universal Oil Prod Co | Treatment of hydrocarbon oils |
| US2344789A (en) * | 1940-09-30 | 1944-03-21 | Universal Oil Prod Co | Destructive hydrogenation of hydrocarbon oils |
| US2357495A (en) * | 1940-10-19 | 1944-09-05 | Universal Oil Prod Co | Treatment of hydrocarbons |
| US2324762A (en) * | 1940-11-30 | 1943-07-20 | Standard Oil Dev Co | Isomerization process |
| GB550480A (en) * | 1941-04-02 | 1943-01-11 | Anglo Iranian Oil Co Ltd | Improvements relating to the production of isoparaffins |
| US2366699A (en) * | 1941-09-20 | 1945-01-09 | Gulf Oil Corp | Production of isoparaffins |
| US2334553A (en) * | 1941-11-08 | 1943-11-16 | Standard Oil Dev Co | Apparatus and process for catalytic reactions of low boiling hydrocarbons |
Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3172834A (en) * | 1965-03-09 | Process for manufacturing gasoline by blending the hydrocracked gasoline with the dehydrogenated and alkyl- ated products obtained from the hy- drocracking stage | ||
| US2709151A (en) * | 1950-12-01 | 1955-05-24 | Basf Ag | Process for the recovery of gasoline from petroleum oils or crude residues by destructive hydrogenation with the use of a catalyst |
| US2946738A (en) * | 1957-07-01 | 1960-07-26 | Phillips Petroleum Co | Hydrocracking a gas oil with a presulfided catalyst consisting of oxides of vanadium, cobalt and molybdenum on gamma alumina |
| US2915571A (en) * | 1957-11-13 | 1959-12-01 | Universal Oil Prod Co | Isomerization of saturated hydrocarbons |
| US2970954A (en) * | 1958-02-14 | 1961-02-07 | Socony Mobil Oil Co Inc | Selective demethylation of hydrocarbon mixtures containing saturated and unsaturated hydrocarbons |
| US3047490A (en) * | 1958-11-04 | 1962-07-31 | Phillips Petroleum Co | Hydrocracking process |
| US3044953A (en) * | 1959-03-30 | 1962-07-17 | California Research Corp | Removal of an undecane-rich fraction from a hydrocarbon conversion process recycle |
| US3153627A (en) * | 1960-04-04 | 1964-10-20 | Gulf Research Development Co | Catalytic process |
| US3110662A (en) * | 1960-06-24 | 1963-11-12 | California Research Corp | Catalytic conversion process for the production of low freezing point fuels |
| US3153100A (en) * | 1960-06-28 | 1964-10-13 | California Research Corp | Process for converting monoalkyl-substituted monocyclic naphthenes |
| US3128243A (en) * | 1960-06-29 | 1964-04-07 | California Research Corp | Hydrocracking process with an aluminanickel sulfide catalyst activated with bf3 |
| US3135682A (en) * | 1961-01-03 | 1964-06-02 | California Research Corp | Process for producing gasoline from a cracked feed stock by catalytic hydrocracking |
| US3242067A (en) * | 1961-10-31 | 1966-03-22 | Exxon Research Engineering Co | Fluid hydrogenative cracking process with the use of unsulfided metallic nickel on a cracking catalyst support |
| US3130240A (en) * | 1961-11-16 | 1964-04-21 | Phillips Petroleum Co | Process for the activation of hydrogenation catalysts |
| US3180818A (en) * | 1962-12-03 | 1965-04-27 | California Research Corp | Two stage hydrocarbon conversion process with hydrocracking in both stages to produce a high octane gasoline |
| US3209052A (en) * | 1963-01-17 | 1965-09-28 | Shell Oil Co | Integrated hydration-isomerization process |
| US3303124A (en) * | 1964-12-24 | 1967-02-07 | Shell Oil Co | Catalytic hydrocracking of naphthas with the use of a catalyst composite comprising copper on a siliceous support |
| US3385782A (en) * | 1966-05-06 | 1968-05-28 | Chevron Res | Production of light hydrocarbon gases by hydrocracking high boiling hydrocarbons |
| US3432568A (en) * | 1966-06-20 | 1969-03-11 | Mobil Oil Corp | Upgrading of hydrocarbons in the presence of a mixed alumino-silicate and metal catalyst |
| US3530060A (en) * | 1968-12-30 | 1970-09-22 | Mobil Oil Corp | Gasoline manufacture |
| US4101592A (en) * | 1977-02-04 | 1978-07-18 | Phillips Petroleum Company | Catalytic hydrogenation |
| US5246567A (en) * | 1992-02-10 | 1993-09-21 | Amoco Corporation | Benzene removal in an isomerization process |
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