US2564268A - Catalytic oil cracking - Google Patents
Catalytic oil cracking Download PDFInfo
- Publication number
- US2564268A US2564268A US785199A US78519947A US2564268A US 2564268 A US2564268 A US 2564268A US 785199 A US785199 A US 785199A US 78519947 A US78519947 A US 78519947A US 2564268 A US2564268 A US 2564268A
- Authority
- US
- United States
- Prior art keywords
- catalyst
- bauxite
- conversion
- catalytic
- gasoline
- 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
Links
- 238000005336 cracking Methods 0.000 title claims description 10
- 230000003197 catalytic effect Effects 0.000 title description 14
- 239000003054 catalyst Substances 0.000 claims description 33
- 239000003921 oil Substances 0.000 claims description 23
- 238000000034 method Methods 0.000 claims description 19
- 229910001570 bauxite Inorganic materials 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 17
- DLYUQMMRRRQYAE-UHFFFAOYSA-N tetraphosphorus decaoxide Chemical compound O1P(O2)(=O)OP3(=O)OP1(=O)OP2(=O)O3 DLYUQMMRRRQYAE-UHFFFAOYSA-N 0.000 claims description 16
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 claims description 15
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 claims description 11
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical class [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- 229910052739 hydrogen Inorganic materials 0.000 claims 1
- 239000001257 hydrogen Substances 0.000 claims 1
- 239000000446 fuel Substances 0.000 description 10
- 229910011255 B2O3 Inorganic materials 0.000 description 9
- MRMOZBOQVYRSEM-UHFFFAOYSA-N tetraethyllead Chemical compound CC[Pb](CC)(CC)CC MRMOZBOQVYRSEM-UHFFFAOYSA-N 0.000 description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 8
- 238000009835 boiling Methods 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 239000003208 petroleum Substances 0.000 description 8
- 238000000151 deposition Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 230000008021 deposition Effects 0.000 description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000000499 gel Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 description 2
- 229910052794 bromium Inorganic materials 0.000 description 2
- 238000004523 catalytic cracking Methods 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000002035 prolonged effect Effects 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000011149 active material Substances 0.000 description 1
- 235000013844 butane Nutrition 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000002301 combined effect Effects 0.000 description 1
- 230000006735 deficit Effects 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 229910000286 fullers earth Inorganic materials 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical class CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/02—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils characterised by the catalyst used
- C10G11/04—Oxides
Definitions
- This invention relates to an improved process for the catalytic cracking of hydrocarbon oils to produce a high yield of high octane gasoline motor fuel. In another aspect it relates to a process for the catalytic cracking of hydrocarbon oils in which the yield of gaseous by-products is low. In another aspect it relates to such a process in which the amount of carbon deposition is low.
- gasoline motor fuel is the petroleum product in greatest demand, efforts are being constantly made to devise methods or processes to produce this gasoline motor fuel 7 800--1400 F., a good catalyst must be able to withstand exposure to high temperatures without serious impairment of efficiency. The process must allow a high throughput of high-boiling point oil and return a high yield of high octane gasoline. The amount of dry gas (propane and lighter hydrocarbons) formed should be low. As carbon from the cracking builds up on the catalyst, the catalytic activity drops, and'the catalyst must be taken out of service for regeneration when the activity drops to a certain predetermined level.
- the rate of carbon deposition be as low as is consistent with economical operation of the process.
- the carbon deposition increases with an increase in the space velocity'at' constant conversion or with an increase in per cent conversion at constant space velocity, so an optimum balance between these important factors must be maintained. 7
- catalysts having a high order of activity for converting high-boiling hydrocarbon oils into gasoline with'a superior octane rating may be prepared by impregnating a solid, absorbent, catalytically active material with a mixed B203 and P205 promoter.
- the principal object of our invention is to provide an improved process for the catalytic conversion of high-boiling petroleum oils ,into high octane gasoline motor fuels at a high yield through the use of the catalyst comprising a major constituent selected from the group consisting of bauxite, fullers earth, acid treated montmorillonite clay, and the synthetically prepared alumina, silica, and silica-alumina gels supporting a minor proportion of boric oxide and phosphorus pentoxide.
- Another object of our invention is to provide a process for the catalytic conversion of high-boiling point petroleum oils into high octane gasoline motor fuels at a high yield and without forming an unduly high amount of dry gas.
- Another object of our invention is to provide a process for the catalytic conversion of highboiling point petroleum oils into high octane gasoline motor fuels at a high yield and without depositing an unduly high amount of carbon.
- Another object of our invention is to provide a process for the catalytic conversion of highboiling point petroleum oils into high octane gasoline motor fuels, in which process, the catalyst is maintained at high activity and high efilciency for longer periods.
- Another object is to provide a new and improved catalyst for the conversion of hydrocarbon oils into high octane gasoline.
- Another object is to provide a method of preparing said catalyst.
- catalyst from 0.1 to 10% by weight of boric oxide and from 0.1 to 10% by weight of phosphorus pentoxide.
- the high-boiling point 011 is substantially vaporized in a preheater, passed into a catalytic reactor where it is contacted with the catalyst for the desired time, and then passed tirely.
- the charge is'vaporized and superheated with as little thermal decomposition as possible to a temperature in the range of 850-1100 F.
- a pressure of 10-300 pounds per square. inch gauge at the preheater outlet is preferred.
- the vaporized petroleum oil' ispassedfrom the preheater into the catalytic reactor where it contacts the catalytic mass at a space velocityof from 01-10 liquid volumes ofpetroleum' oil per volume of catalytic mass per hour.
- the amount of conversion is partially controlled by the. length of time the oil is exposedto the catalyst. However, if the velocity is low, the process is uneconomical beeausethe total' product" will be low and the rate of carbon deposition increases: If
- the initial high activity of the catalyst It was calculated that the promoter content was 1.05 weight per cent of P205 and 1.05 per cent of B203.
- a catalyst of bauxite containing P205 alone in the amount of 1.4 weight per cent and one containing B203 alone in the amount of 2.0 weight per cent were prepared in a similar manner.
- Example II The four catalysts prepared in Example I were tested in a fixed bed hydrocarbon cracking system charged with an oil having a boiling point essentially above that of gasoline. A catalyst temperature of 10i5 R, a pressure of 85 pounds per square inch gauge, and an operating period of 3 hours. were used. The space velocities, measured in terms of liquid volumes of oil per volume of catalyst per hour, were held constant for" all tests. The results are shown in Table I.
- the activity index is the comparison of the per cent conversion obtained with each catalyst compared with that of the original bauxite.
- the efiluent gases from. thecatalytic reactor are led into a separator where the gasoline motor fuel, dry gas, and butanes are removed. If desired, the high-boiling fraction maybe recycled through the system by introducing it back into the preheater.
- the following examples serve to illus trate further the advantages of our invention.
- A250 gram sampleof the calcined bauxite was soaked for 1 hour in 250 ml. or" solutioncontaining 10.1'grams of HSPO4 and 1L7 grams of I-Is'B'Os. The mass was then drained for "1 hour, air dried for 3 days, oven dried "at 482 F; for hours, and
- the bauxite impregnated with B203 and the bauxite impregnated with P205 catalyst has a higher activity indexthan the untreated bauxite.
- Thecatalytic efiect of our catalyst is more than the combined effect produced by B203 and P205 separately.
- EXAMPLE III Another comparison was made using a. high grade bauxite'and the same bauxite impregnated with 3203' and P205 in minor'amounts for cracking a virgin gas oil.
- the octane numbers were run on the product gasoline clear and with 1 and 3 'ml. of tetraethyl lead per'gallon of gasoline; The operating conditions and results are" shown in Table II.
- a process for the conversion of hydrocarbon oils to produce a high octane gasoline which comprises passing said oil at a cracking temperature and pressure through a cracking zone containing an active catalyst comprising bauxite supporting impregnated on'its surface .1 to weight per cent of phosphorus pentoxide and boron trioxide as such and maintaining said hydrocarbon oil in contact with said catalyst for a period of time sufiicient to obtain the desired conversion thereof.
- a process for cracking hydrocarbon oils which comprises contacting the said hydrocarbon oil at a temperature of 800 F. to 1400 F., a pressure between 10 and 300 pounds per square inch gauge, and a space velocity of from 0.1 to 10 volumes of liquid charge per volume of catalyst per hour with an active catalytic mass comprising bauxite as a major constituent supporting impregnated thereon as such 0.1 to 10 weight per cent of boron trioxide and 0,1 to 10 weight per cent of phosphorus pentoxide.
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)
- Catalysts (AREA)
Description
Patented Aug. 14, 1 951 CATALYTIC OIL CRACKING Eugene V. Mathy and CarlJ. Helmers, Bartlesville, kla., assignors to Phillips Petroleum Company, a corporation of Delaware No Drawing. Application November 10, 1947,
.Serial No. 785,199
3 Claims. (01. 196 52) This invention relates to an improved process for the catalytic cracking of hydrocarbon oils to produce a high yield of high octane gasoline motor fuel. In another aspect it relates to a process for the catalytic cracking of hydrocarbon oils in which the yield of gaseous by-products is low. In another aspect it relates to such a process in which the amount of carbon deposition is low.
In still another aspect, it relates to an improved catalyst and a method ofpreparation of same.
In the production of gasoline motor fuel from petroleum, a small amount may be obtained by simple fractionation. Since gasoline motor fuel is the petroleum product in greatest demand, efforts are being constantly made to devise methods or processes to produce this gasoline motor fuel 7 800--1400 F., a good catalyst must be able to withstand exposure to high temperatures without serious impairment of efficiency. The process must allow a high throughput of high-boiling point oil and return a high yield of high octane gasoline. The amount of dry gas (propane and lighter hydrocarbons) formed should be low. As carbon from the cracking builds up on the catalyst, the catalytic activity drops, and'the catalyst must be taken out of service for regeneration when the activity drops to a certain predetermined level. Therefore, it is desirable that the rate of carbon deposition be as low as is consistent with economical operation of the process. However, the carbon deposition increases with an increase in the space velocity'at' constant conversion or with an increase in per cent conversion at constant space velocity, so an optimum balance between these important factors must be maintained. 7
We have found that catalysts having a high order of activity for converting high-boiling hydrocarbon oils into gasoline with'a superior octane rating may be prepared by impregnating a solid, absorbent, catalytically active material with a mixed B203 and P205 promoter.
The principal object of our invention is to provide an improved process for the catalytic conversion of high-boiling petroleum oils ,into high octane gasoline motor fuels at a high yield through the use of the catalyst comprising a major constituent selected from the group consisting of bauxite, fullers earth, acid treated montmorillonite clay, and the synthetically prepared alumina, silica, and silica-alumina gels supporting a minor proportion of boric oxide and phosphorus pentoxide.
Another object of our invention is to provide a process for the catalytic conversion of high-boiling point petroleum oils into high octane gasoline motor fuels at a high yield and without forming an unduly high amount of dry gas.
Another object of our invention is to provide a process for the catalytic conversion of highboiling point petroleum oils into high octane gasoline motor fuels at a high yield and without depositing an unduly high amount of carbon.
Another object of our invention is to provide a process for the catalytic conversion of highboiling point petroleum oils into high octane gasoline motor fuels, in which process, the catalyst is maintained at high activity and high efilciency for longer periods.
Another object is to provide a new and improved catalyst for the conversion of hydrocarbon oils into high octane gasoline.
Another object is to provide a method of preparing said catalyst.
Numerous other objects and advantages of our invention will be apparent to those skilled in the art upon reading the following specification and the accompanying claims.
OPERATIONS not as economical, we prefer to employ in this.
catalyst from 0.1 to 10% by weight of boric oxide and from 0.1 to 10% by weight of phosphorus pentoxide.
In its operation, the high-boiling point 011 is substantially vaporized in a preheater, passed into a catalytic reactor where it is contacted with the catalyst for the desired time, and then passed tirely. The charge is'vaporized and superheated with as little thermal decomposition as possible to a temperature in the range of 850-1100 F. A pressure of 10-300 pounds per square. inch gauge at the preheater outlet is preferred.
The vaporized petroleum oil' ispassedfrom the preheater into the catalytic reactor where it contacts the catalytic mass at a space velocityof from 01-10 liquid volumes ofpetroleum' oil per volume of catalytic mass per hour. The amount of conversion is partially controlled by the. length of time the oil is exposedto the catalyst. However, if the velocity is low, the process is uneconomical beeausethe total' product" will be low and the rate of carbon deposition increases: If
the initial high activity of the catalyst. It was calculated that the promoter content was 1.05 weight per cent of P205 and 1.05 per cent of B203.
A catalyst of bauxite containing P205 alone in the amount of 1.4 weight per cent and one containing B203 alone in the amount of 2.0 weight per cent were prepared in a similar manner.
EXAMPLE II The four catalysts prepared in Example I were tested in a fixed bed hydrocarbon cracking system charged with an oil having a boiling point essentially above that of gasoline. A catalyst temperature of 10i5 R, a pressure of 85 pounds per square inch gauge, and an operating period of 3 hours. were used. The space velocities, measured in terms of liquid volumes of oil per volume of catalyst per hour, were held constant for" all tests. The results are shown in Table I. The activity index is the comparison of the per cent conversion obtained with each catalyst compared with that of the original bauxite.
Table I e Bauxite Bauxite Bauxite 20% B203 not B2O3':O1-505%.
Space Velocity -l 1. 8 1.' 8 1. 8" 1. 8 Per Cent Conversion. 51. 2 53. 9 52. 3 56. 5 Dry Gas, wt. per cent 12. 9 13.4 12. 8- 14.1 Birtanes, vol. per cent 6. 2 7. 4 7. 8 8. 1 Carbon, wt. per cent 1.8 2. 0 2. 8 3. 4 Gasoline:
Yield, vol. per cent"..- 35. 0 36. 3' 34. 4 36. 2
ASTM Octane N0 75. 6 76. 6' 77. 2 76. 8
Bromine N o 91 96 88 81 Activity Index.. 100 105 102 110 silica-alumina gel which material has been im-- pregnated with a, minor proportion of boron trioxide and phosphorus pentoxideas a combination promoter ma be used.
The efiluent gases: from. thecatalytic reactor are led into a separator where the gasoline motor fuel, dry gas, and butanes are removed. If desired, the high-boiling fraction maybe recycled through the system by introducing it back into the preheater. The following examples serve to illus trate further the advantages of our invention.
EXAMPLE I Samples of our catalysts were prepared 'as-follows A portion of bauxitecontaining less than 3-per' cent of iron and having'a particle size of 844' mesh was calcined at a temperature of 700-900 for a period of about 10 hours to reducethe water content below 5 per cent.
A250 gram sampleof the calcined bauxite was soaked for 1 hour in 250 ml. or" solutioncontaining 10.1'grams of HSPO4 and 1L7 grams of I-Is'B'Os. The mass was then drained for "1 hour, air dried for 3 days, oven dried "at 482 F; for hours, and
heat-treated for"168*h0urs at1500 F.- to kill The bauxite impregnated with B203 and the bauxite impregnated with P205 catalyst has a higher activity indexthan the untreated bauxite. Thecatalytic efiect of our catalyst is more than the combined effect produced by B203 and P205 separately.
EXAMPLE III Another comparison was made using a. high grade bauxite'and the same bauxite impregnated with 3203' and P205 in minor'amounts for cracking a virgin gas oil. The octane numbers were run on the product gasoline clear and with 1 and 3 'ml. of tetraethyl lead per'gallon of gasoline; The operating conditions and results are" shown in Table II.
Table [I Bauxite Bauxite+B20 +PiO5 Pressure 85 Temperature, F 980 980 Conversion, Vol. Per Cent I 52' 54 Gasoline:.
Yield, Vol Per'Cent' 38.3 35 7 Bromine N o 74 70 Cycle Stock, VOL- 48.0 45. 4 Dry- Gasfwt; PerOent; 9. 8 11.5 Tests. for tetraethyl lead responsez. ASTM Octane-Numbers 0 ml. TEL pergal 74. 1 76:5 1 ml. TEL per gal 78. 5 80. 0 3 ml. TEL per gal 81.8 82. 7 ResearchOctane Numbers 0 mlJTEL per gel H. 82.3 86.3 1 ml. TEL per'gali- 88.7 92.0 3 m1. TEL per gal= 92. 4 94.1
The higher conversion obtained by using our catalyst more than'compen'sates for the'slightly lower gasoline yield. The superiority of our catalyst'is clearly shownin the higher'octane rating of the gasoline produced? From the foregoing examples, it is apparent that this process has many advantages. The catalytic activity is not impaired by prolonged exposure to high temperatures. When our catalyst is employed a gasoline of a high octane rat ing is produced. The low rate of carbon deposition means prolonged life of the catalyst at high activity. Due to the high catalytic activity as reflected in the high conversion ratio, our catalyst permits a higher space velocity or throughput than is possible with the other catalysts tested. This means that more high-boiling point petroleum oil may be processed in less time and with a high yield of high octane gasoline motor fuel.
In the practicing of this invention it is obvious that variations in the arrangement may be made without invention. For instance, instead of the fixed-bed catalyst described in the examples, a fluidized bed may be used. This invention embraces such other obvious variations and modifications as come within the scope thereof. This invention is limited only by the following claims.
Having fully described our invention, we claim:
1. A process for the conversion of hydrocarbon oils to produce a high octane gasoline which comprises passing said oil at a cracking temperature and pressure through a cracking zone containing an active catalyst comprising bauxite supporting impregnated on'its surface .1 to weight per cent of phosphorus pentoxide and boron trioxide as such and maintaining said hydrocarbon oil in contact with said catalyst for a period of time sufiicient to obtain the desired conversion thereof.
2. A process for cracking hydrocarbon oils which comprises contacting the said hydrocarbon oil at a temperature of 800 F. to 1400 F., a pressure between 10 and 300 pounds per square inch gauge, and a space velocity of from 0.1 to 10 volumes of liquid charge per volume of catalyst per hour with an active catalytic mass comprising bauxite as a major constituent supporting impregnated thereon as such 0.1 to 10 weight per cent of boron trioxide and 0,1 to 10 weight per cent of phosphorus pentoxide.
REFERENCE S CITED The following references are of record in the file of this patent:
UNITED STATES PATENTS Number Name Date 2,109,866 Moser Mar. 1, 1938 2,341,363 Connolly Feb. 8, 1944 2,398,819 Cook Apr. 23, 1946 2,441,493 Krug May 11, 1948 2,443,402 Schulze June 15, 1948 2,480,672 Plank Aug. 30, 1949 OTHER REFERENCES Mellor, Comprehensive Treatise on Inorganic and Theoretical Chemistry, vol. 5, page 147.
Handbook of Chem. & Physics Hadgman and Lange, 16th edition, page 198.
Claims (1)
1. A PROCESS FOR THE CONVERSION OF HYDROGEN OILS TO A PRODUCE A HIGH OCTANE GASOLINE WHICH COMPRISES PASSING SAID OIL AT A CRACKING TEMPERATURE AND PRESSURE THROUGH A CRACKING ZONE CONTAINING AN ACTIVE CATALYST COMPRISING BAUXITE SUPPORTING IMPREGNATED ON ITS SURFACE .1 TO 10 WEIGHT PER CENT OF PHOSPHORUS PENTOXIDE AND BORON TRIOXIDE AS SUCH AND MAINTAINING SAID HYDROCARBON OIL IN CONTACT WITH SAID CATALYST DESIRED CONVERSION THEREOF.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US785199A US2564268A (en) | 1947-11-10 | 1947-11-10 | Catalytic oil cracking |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US785199A US2564268A (en) | 1947-11-10 | 1947-11-10 | Catalytic oil cracking |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2564268A true US2564268A (en) | 1951-08-14 |
Family
ID=25134736
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US785199A Expired - Lifetime US2564268A (en) | 1947-11-10 | 1947-11-10 | Catalytic oil cracking |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2564268A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2938001A (en) * | 1956-12-13 | 1960-05-24 | Universal Oil Prod Co | Catalyst composite |
| US3030300A (en) * | 1957-12-11 | 1962-04-17 | California Research Corp | Catalytic cracking with an attrition resistant catalyst |
| US3261878A (en) * | 1961-02-09 | 1966-07-19 | Autothermal cracking of liquid hydrocarbons | |
| US3883442A (en) * | 1972-05-19 | 1975-05-13 | Union Oil Co | Non-shrinking alumina-based catalyst compositions |
| US4295955A (en) * | 1980-03-10 | 1981-10-20 | Uop Inc. | Attenuation of metal contaminants on cracking catalyst with a boron compound |
| US4334979A (en) * | 1980-04-11 | 1982-06-15 | Phillips Petroleum Company | Hydrocarbon cracking process using a catalyst containing germanium |
| US4386015A (en) * | 1980-04-11 | 1983-05-31 | Phillips Petroleum Company | Hydrocarbon cracking zeolitic catalyst |
| US4439536A (en) * | 1980-04-11 | 1984-03-27 | Phillips Petroleum Company | Hydrocarbon cracking catalyst |
| US4490476A (en) * | 1983-06-28 | 1984-12-25 | Rohm And Haas Company | Catalyst for the preparation of α,β-unsaturated compounds |
| US5151394A (en) * | 1991-01-25 | 1992-09-29 | Mobil Oil Corporation | Cracking catalysts |
| US5300215A (en) * | 1991-01-25 | 1994-04-05 | Mobil Oil Corporation | Catalytic cracking with a catalyst comprising a boron phosphate matrix |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2109866A (en) * | 1934-09-21 | 1938-03-01 | Shell Dev | Treating of motor fuels |
| US2341363A (en) * | 1940-12-27 | 1944-02-08 | Standard Oil Dev Co | Conversion of hydrocarbon oils |
| US2398819A (en) * | 1942-03-20 | 1946-04-23 | Texas Co | Conversion of hydrocarbons |
| US2441493A (en) * | 1947-06-10 | 1948-05-11 | Atlantic Refining Co | Desulfurization of hydrocarbons with boron phosphate-alumina catalyst |
| US2443402A (en) * | 1942-02-10 | 1948-06-15 | Phillips Petroleum Co | Process for hydrocarbon conversion |
| US2480672A (en) * | 1944-08-12 | 1949-08-30 | Socony Vacuum Oil Co Inc | Process for forming porous glass and composition thereof |
-
1947
- 1947-11-10 US US785199A patent/US2564268A/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2109866A (en) * | 1934-09-21 | 1938-03-01 | Shell Dev | Treating of motor fuels |
| US2341363A (en) * | 1940-12-27 | 1944-02-08 | Standard Oil Dev Co | Conversion of hydrocarbon oils |
| US2443402A (en) * | 1942-02-10 | 1948-06-15 | Phillips Petroleum Co | Process for hydrocarbon conversion |
| US2398819A (en) * | 1942-03-20 | 1946-04-23 | Texas Co | Conversion of hydrocarbons |
| US2480672A (en) * | 1944-08-12 | 1949-08-30 | Socony Vacuum Oil Co Inc | Process for forming porous glass and composition thereof |
| US2441493A (en) * | 1947-06-10 | 1948-05-11 | Atlantic Refining Co | Desulfurization of hydrocarbons with boron phosphate-alumina catalyst |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2938001A (en) * | 1956-12-13 | 1960-05-24 | Universal Oil Prod Co | Catalyst composite |
| US3030300A (en) * | 1957-12-11 | 1962-04-17 | California Research Corp | Catalytic cracking with an attrition resistant catalyst |
| US3261878A (en) * | 1961-02-09 | 1966-07-19 | Autothermal cracking of liquid hydrocarbons | |
| US3883442A (en) * | 1972-05-19 | 1975-05-13 | Union Oil Co | Non-shrinking alumina-based catalyst compositions |
| US4295955A (en) * | 1980-03-10 | 1981-10-20 | Uop Inc. | Attenuation of metal contaminants on cracking catalyst with a boron compound |
| US4334979A (en) * | 1980-04-11 | 1982-06-15 | Phillips Petroleum Company | Hydrocarbon cracking process using a catalyst containing germanium |
| US4386015A (en) * | 1980-04-11 | 1983-05-31 | Phillips Petroleum Company | Hydrocarbon cracking zeolitic catalyst |
| US4439536A (en) * | 1980-04-11 | 1984-03-27 | Phillips Petroleum Company | Hydrocarbon cracking catalyst |
| US4490476A (en) * | 1983-06-28 | 1984-12-25 | Rohm And Haas Company | Catalyst for the preparation of α,β-unsaturated compounds |
| US5151394A (en) * | 1991-01-25 | 1992-09-29 | Mobil Oil Corporation | Cracking catalysts |
| US5300215A (en) * | 1991-01-25 | 1994-04-05 | Mobil Oil Corporation | Catalytic cracking with a catalyst comprising a boron phosphate matrix |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US3788977A (en) | Hydrocarbon cracking with both azeolite and pt-u-alumina in the matrix | |
| US2849383A (en) | Catalytic composition and hydrocarbon conversion therewith | |
| US2564268A (en) | Catalytic oil cracking | |
| Turkevich | Zeolites as catalysts. I | |
| US2422884A (en) | Isomerizing olefins using boric oxide on alumina as catalyst | |
| JPH0344055B2 (en) | ||
| US2341567A (en) | Process for removing fluorine from hydrocarbon distillates | |
| US2668142A (en) | Reforming process and catalysts | |
| US2461069A (en) | Simultaneous catalytic cracking and desulfurization of hydrocarbons | |
| US2407918A (en) | Catalytic conversion of carbonaceous materials | |
| US3542671A (en) | Hydroisomerization of olefins to isoparaffins | |
| Hay et al. | Catalytic isomerization of 1-hexene | |
| US2242553A (en) | Treatment of hydrocarbons | |
| US2328178A (en) | Manufacture of gasoline | |
| US2469733A (en) | Cracking oil with aerogel catalysts | |
| US2926207A (en) | Isomerization catalysts and process | |
| US2892003A (en) | Isomerization of paraffin hydrocarbons | |
| US2109866A (en) | Treating of motor fuels | |
| US2339248A (en) | Manufacture of catalysts | |
| US3344059A (en) | Conversion of hydrocarbons to gasoline with a zunyite-containing catalyst composite | |
| US2480494A (en) | Catalytic oil cracking | |
| US2865842A (en) | Cracking of a hydrocarbon oil with a silica-alumina-tungsten phosphate catalyst composite | |
| US2347216A (en) | Producing gasolines | |
| US3023159A (en) | Controlled hydrocracking process | |
| US3216923A (en) | Hydrocarbon conversion process and catalyst therefor |