GB766404A - A process for the production of gasoline and related lighter products by means of hydrogenation and catalytic cracking - Google Patents
A process for the production of gasoline and related lighter products by means of hydrogenation and catalytic crackingInfo
- Publication number
- GB766404A GB766404A GB35977/54A GB3597754A GB766404A GB 766404 A GB766404 A GB 766404A GB 35977/54 A GB35977/54 A GB 35977/54A GB 3597754 A GB3597754 A GB 3597754A GB 766404 A GB766404 A GB 766404A
- Authority
- GB
- United Kingdom
- Prior art keywords
- distillate
- gasoline
- section
- hydrogen
- naphtha
- 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
Links
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
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
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)
Abstract
<PICT:0766404/III/1> In a process for cracking petroleum distillate oils boiling above the gasoline range, the oil is divided into two portions, one of these portions is subjected to catalytic hydrogenation under such conditions that there is an uptake of hydrogen amounting to between 100 and 700 cubic feet per barrel of oil-being-hydrogenated without any material lowering of the average molecular weight of the oil, and the hydrogenated oil and the unhydrogenated oil are then submitted to catalytic cracking in the same reactor, whereby gasoline is produced. The required hydrogen may be derived from a naphtha-hydroforming unit. Crude desalted California petroleum (1000 barrels) is topped in section 1 to give straight-run gasoline and a residue. The gasoline is fractionated in section 2 to produce light gasoline, which is removed at B, and also 200 DEG -400 DEG F. naphtha. This naphtha is passed to section 3 wherein it is hydroformed, at a temperature of 800 DEG to 920 DEG F. and a pressure of 700 p.s.i., in the presence of hydrogen and a platinum catalyst deposited on HF-treated alumina. The hydroformed naphtha, which has an octane number of 89, is removed at C. Hydrogen, 730 cubic feet per barrel of naphtha is also produced in section 3. The residue from the topping section 1 is passed to section 4 where it is vacuum-flashed to give a distillate and a pitch-residue. The distillate is passed to fractionator 5, wherein it is separated into light and heavy fractions (275 barrels of each). The lower boiling fraction is passed to unit 6 wherein it is hydrogenated with the product gas from platforming unit 3. The hydrogenation is effected at a temperature of 710 DEG F. and a pressure of 750 p.s.i., and in the presence of a tungsten nickel sulphide catalyst. The hydrogen uptake is 284 cubic feet per barrel of light flashed distillate. The hydrogenated light distillate is combined with the heavy flashed distillate; and the mixture is cracked in the vapour phase at 930 DEG F. in unit 7 which contains synthetic silica-alumina catalyst. The increase in the value of the products is more than 50 per cent higher than for the prior art process where the total flashed distillate is hydrogenated with the same hydrogen consumption.
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US398031A US2792336A (en) | 1953-12-14 | 1953-12-14 | Production of lighter hydrocarbons from petroleum oils involving hydrogenation and catalytic cracking |
Publications (1)
Publication Number | Publication Date |
---|---|
GB766404A true GB766404A (en) | 1957-01-23 |
Family
ID=23573718
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB35977/54A Expired GB766404A (en) | 1953-12-14 | 1954-12-13 | A process for the production of gasoline and related lighter products by means of hydrogenation and catalytic cracking |
Country Status (5)
Country | Link |
---|---|
US (1) | US2792336A (en) |
BE (1) | BE534075A (en) |
DE (1) | DE1004756B (en) |
FR (1) | FR1121932A (en) |
GB (1) | GB766404A (en) |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2944003A (en) * | 1954-10-29 | 1960-07-05 | Shell Oil Co | Production of aviation gasoline |
US2939832A (en) * | 1955-11-22 | 1960-06-07 | Shell Oil Co | Blended gasolines |
US2895897A (en) * | 1956-08-28 | 1959-07-21 | Shell Dev | Production of gasoline from petroleum residues |
US2964463A (en) * | 1956-12-10 | 1960-12-13 | Pure Oil Co | Upgrading hydrocarbon oils in the presence of hydrogen with a tungsten oxide, molybdenum oxide on silica-alumina catalyst composite |
US2915457A (en) * | 1957-06-14 | 1959-12-01 | Shell Dev | Process for the conversion of heavy residual oils |
US2914457A (en) * | 1957-06-28 | 1959-11-24 | Texaco Inc | Petroleum refining process |
US2925374A (en) * | 1958-05-19 | 1960-02-16 | Exxon Research Engineering Co | Hydrocarbon treating process |
US2998380A (en) * | 1959-02-27 | 1961-08-29 | Standard Oil Co | Catalytic cracking of reduced crudes |
JPS5829885A (en) * | 1981-08-18 | 1983-02-22 | Mitsubishi Oil Co Ltd | Preparation of pitch used as raw material for carbon fiber |
US4565620A (en) * | 1984-05-25 | 1986-01-21 | Phillips Petroleum Company | Crude oil refining |
US4713221A (en) * | 1984-05-25 | 1987-12-15 | Phillips Petroleum Company | Crude oil refining apparatus |
Family Cites Families (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2205434A (en) * | 1937-11-30 | 1940-06-25 | Process Management Co Inc | Treatment of hydrocarbon oils |
US2360622A (en) * | 1943-04-30 | 1944-10-17 | Standard Oil Dev Co | Method of producing aviation gasoline |
US2663676A (en) * | 1951-03-16 | 1953-12-22 | Standard Oil Dev Co | Catalyst recovery |
US2671754A (en) * | 1951-07-21 | 1954-03-09 | Universal Oil Prod Co | Hydrocarbon conversion process providing for the two-stage hydrogenation of sulfur containing oils |
-
0
- BE BE534075D patent/BE534075A/xx unknown
-
1953
- 1953-12-14 US US398031A patent/US2792336A/en not_active Expired - Lifetime
-
1954
- 1954-12-13 GB GB35977/54A patent/GB766404A/en not_active Expired
- 1954-12-13 DE DEN9896A patent/DE1004756B/en active Pending
- 1954-12-13 FR FR1121932D patent/FR1121932A/en not_active Expired
Also Published As
Publication number | Publication date |
---|---|
DE1004756B (en) | 1957-03-21 |
US2792336A (en) | 1957-05-14 |
FR1121932A (en) | 1956-08-28 |
BE534075A (en) |
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