US2686150A - Catalytic cracking of petroleum hydrocarbons - Google Patents
Catalytic cracking of petroleum hydrocarbons Download PDFInfo
- Publication number
- US2686150A US2686150A US70597A US7059749A US2686150A US 2686150 A US2686150 A US 2686150A US 70597 A US70597 A US 70597A US 7059749 A US7059749 A US 7059749A US 2686150 A US2686150 A US 2686150A
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- United States
- Prior art keywords
- feedstock
- gas oil
- gasoline
- range
- wax distillate
- 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
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- 239000003208 petroleum Substances 0.000 title claims description 14
- 238000004523 catalytic cracking Methods 0.000 title claims description 11
- 229930195733 hydrocarbon Natural products 0.000 title description 3
- 150000002430 hydrocarbons Chemical class 0.000 title description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 26
- 239000003502 gasoline Substances 0.000 claims description 26
- 239000005864 Sulphur Substances 0.000 claims description 23
- 238000009835 boiling Methods 0.000 claims description 22
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 13
- 239000002283 diesel fuel Substances 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- 229910052739 hydrogen Inorganic materials 0.000 claims description 8
- 239000001257 hydrogen Substances 0.000 claims description 8
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical class [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- 239000003054 catalyst Substances 0.000 claims description 7
- 238000006243 chemical reaction Methods 0.000 claims description 6
- 230000000694 effects Effects 0.000 claims description 6
- 238000005984 hydrogenation reaction Methods 0.000 claims description 6
- 239000007789 gas Substances 0.000 description 28
- 238000005336 cracking Methods 0.000 description 8
- 239000000463 material Substances 0.000 description 6
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 4
- 239000000376 reactant Substances 0.000 description 3
- PAYRUJLWNCNPSJ-UHFFFAOYSA-N Aniline Chemical compound NC1=CC=CC=C1 PAYRUJLWNCNPSJ-UHFFFAOYSA-N 0.000 description 2
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 2
- KYYSIVCCYWZZLR-UHFFFAOYSA-N cobalt(2+);dioxido(dioxo)molybdenum Chemical compound [Co+2].[O-][Mo]([O-])(=O)=O KYYSIVCCYWZZLR-UHFFFAOYSA-N 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000196324 Embryophyta Species 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- 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
Definitions
- This invention relates to the catalytic cracking of petroleum hydrocarbons.
- a process has now been developed of treating a sulphur-containing petroleum feedstock boiling in the wax distillate range or higher for the production of a gas oil fraction of considerably better quality than the cracked gas oil, without any appreciable reduction in the quantity of cracked gasoline based on the weight of the feedstock.
- the process has the further advantage that the cracked gasoline is substantially free from sulphur and has a higher octane number than normal cracked gasoline.
- the process of the invention consists in passing a sulphur-containing petroleum feedstock boiling in the wax distillate range or higher, to a hydrofining stage where it is contacted with a sulphurresistant hydrogenation catalyst in the presence of hydrogen, and under conditions of temperature and pressure to effect conversion of sulphur present in the feedstock into hydrogen sulphide, removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction from the hydrofined feedstock, and passing the residue boiling above the gas oil range to a catalytic cracking stage.
- the amount of gas oil that may be recovered from the hydrofined feedstock depends on the sulphur content of the original feedstock.
- an Egyptian wax distillate has a sulphur content of 1.6 wt. percent, and assuming all the sulphur to be present in the form of sulphides, the sulphur compounds would constitute of the molecules in the feedstock and some or all of the molecules produced from the sulphur compounds by hydrofining would boil outside the range of the original feedstock.
- wax distillate or other petroleum feedstock is fed via pump l and line 2 to the preheater 4 where the reactants are heated to the operating temperature.
- Recycle gas joins the cold feed via line 3 before entering the preheater.
- the heated reactants enter the top of the catalytic reactor 5 and flow downward through the catalyst bed under the predetermined hydrofining conditions of temperature and pressure.
- the desulphurized reactants are then passed through a waste heat boiler or cooler 6 where the temperature is dropped suihciently to ensure that all material boiling above a selected temperature is condensed in the knock out drum or fractionator l.
- the condensed material which comprises the heavy desulphurized fraction is let down to atmospheric pressure via valve 8 and is then fed to the catalytic cracking unit (not shown).
- the vapors leaving knock out drum 1 are further cooled in a waste heat boiler or water cooler l0 and passed into th knock out tower or fra-ctionator H where a bottoms product consisting of the gas oil fraction is removed via cooler l3 and separator I4 to storage.
- the knock out tower or fractionator is fitted with a reboiler l2 and provided with reflux line it.
- the overheads 0f the fractionator l l are cooled by a water cooler H, the gaseous fraction consisting mainly of hydrogen being separated in vessel 18 and recycled via line 3 and booster is to feed line 2.
- the liquid from vessel I8, which consists of light ends is removed via let down valve 29 to storage.
- the yield of cracked gasoline based on the original feedstock has only fallen from 32.5% to 31.4% by weight on the original feedstock, while the octane number of the cracked gasoline has risen from 77.6 to 80.1.
- a process for the production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and. of a good quality diesel fuel without appreciable reduction in the maount of cracked gasoline which may be obtained from the wax distillate, which consists in passing the wax distillate to a hydrofining stage where it is contacted with a sulphurresistant hydrogenation catalyst in the presence of hydrogen and under conditions of temperature and pressure to effect the conversion of organically combined sulphur present in the feedstock into hydrogen sulphide, removing the hydrogen sulphide from the hydrofined feedstock, separating from the hydrofined feedstock a gas oil fraction suitable for use as a diesel fuel passing the residue boiling above the gas oil range to a catalytic cracking stage, and recovering gasoline from the cracked products.
- a process for the production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate which consists in passing the wax distillate to a hydrofining stage where it is contacted with a sulphur-resistant hydrogenation catalyst in the presence of hydrogen and under conditions of temperature and pressure to effect the conversion of organically combined sulphur present in the feedstock into hydrogen sulphide and to increase the content of material boiling within the range 200-400" (3., removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction boiling within the range ZOO-400 C. and suitable for use as a diesel fuel from the hydrofined feedstock passing the residue boiling above the gas oil range to a catalytic cracking stage, and recovering gasoline from the cracked products.
- a process for the production from a sulphur-containing petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate which consists in passing the wax distillate to a hydrofining stage where it is contacted with a catalyst of the cobalt molybdate type in the presence of hydrogen and under conditions of temperature and. pressure to effect conversion of organically combined sulfur present in the feedstock into hydrogen sulphide and to increase the amount of material boiling within the range 200-400 (3., removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction boiling within the range 200-400 C.
- a process for production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate which consists in passing the wax distillate at the rate of 1.0 v./v./hr. to a hydrofining stage maintained at a temperature of about 780 F. and a pressure of 1000 lb./sq. in. together with hydrogen amounting to 4000 cu. ft. per barrel of feedstock,
- the diesel index of said gas oil fraction being considerably higher than the diesel index of the corresponding fraction that can be recovered from the products of catalytically cracking the original feedstock, passing the residue boiling above the gas oil range to a catalytic cracking stage and recovering from the catalytically cracked products a gasoline fraction of increased octane number and in substantially the same amount as would have been recovered from the products of catalytically cracking the feedstock without removal of said gas oil fraction.
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
Patented Aug. 10, 1954- CATALYTIC CRACKING IOF PETROLEUM HYDROCARBONS Frederick William Bertram Porter and John Norman Haresnape, Sunbury-on-Thames, England, assignors to Anglo-Iranian Oil Company Limited, London,
stock corporation England, a British joint- Application January 12, 1949, Serial No. 70,597
Claims priority, application Great Britain January 20, 1948 4 Claims. 1
This invention relates to the catalytic cracking of petroleum hydrocarbons.
It is known that petroleum fractions boiling in the wax distillate range or higher may be catalytically cracked for the production of considerable quantities of gasoline and gas oil. The gas oil produced in this way is, however, of very poor quality and is useful only as boiler fuel, while if the feedstock contains sulphur, as it usually does, the cracked gasoline is also sulphur-containing and requires to be treated for the removal of sulphur.
A process has now been developed of treating a sulphur-containing petroleum feedstock boiling in the wax distillate range or higher for the production of a gas oil fraction of considerably better quality than the cracked gas oil, without any appreciable reduction in the quantity of cracked gasoline based on the weight of the feedstock. The process has the further advantage that the cracked gasoline is substantially free from sulphur and has a higher octane number than normal cracked gasoline.
The process of the invention consists in passing a sulphur-containing petroleum feedstock boiling in the wax distillate range or higher, to a hydrofining stage where it is contacted with a sulphurresistant hydrogenation catalyst in the presence of hydrogen, and under conditions of temperature and pressure to effect conversion of sulphur present in the feedstock into hydrogen sulphide, removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction from the hydrofined feedstock, and passing the residue boiling above the gas oil range to a catalytic cracking stage.
It has been found that the residue boilin above the gas oil range is more susceptible to catalytic cracking than the original feedstock with the result that the yield of gasoline based on the original feedstock is only slightly lower and has a higher octane number. Furthermore, the gasoline produced by catalytically cracking the residue is substantially free from sulphur. There is the further advantage that the hydrofining of the feedstock considerably reduces the corrosion difiiculties experienced in the cracking plant.
The amount of gas oil that may be recovered from the hydrofined feedstock depends on the sulphur content of the original feedstock. As an example, an Iranian wax distillate has a sulphur content of 1.6 wt. percent, and assuming all the sulphur to be present in the form of sulphides, the sulphur compounds would constitute of the molecules in the feedstock and some or all of the molecules produced from the sulphur compounds by hydrofining would boil outside the range of the original feedstock.
The accompanying drawing which forms part of the instant specification and is to be read in conjunction therewith, diagrammatically illustrates one system of apparatus for carrying out the process of the invention.
Referring to the drawing, wax distillate or other petroleum feedstock is fed via pump l and line 2 to the preheater 4 where the reactants are heated to the operating temperature. Recycle gas joins the cold feed via line 3 before entering the preheater. The heated reactants enter the top of the catalytic reactor 5 and flow downward through the catalyst bed under the predetermined hydrofining conditions of temperature and pressure. The desulphurized reactants are then passed through a waste heat boiler or cooler 6 where the temperature is dropped suihciently to ensure that all material boiling above a selected temperature is condensed in the knock out drum or fractionator l. The condensed material which comprises the heavy desulphurized fraction is let down to atmospheric pressure via valve 8 and is then fed to the catalytic cracking unit (not shown). The vapors leaving knock out drum 1 are further cooled in a waste heat boiler or water cooler l0 and passed into th knock out tower or fra-ctionator H where a bottoms product consisting of the gas oil fraction is removed via cooler l3 and separator I4 to storage. The knock out tower or fractionator is fitted with a reboiler l2 and provided with reflux line it. The overheads 0f the fractionator l l are cooled by a water cooler H, the gaseous fraction consisting mainly of hydrogen being separated in vessel 18 and recycled via line 3 and booster is to feed line 2. The liquid from vessel I8, which consists of light ends is removed via let down valve 29 to storage.
The invention will now be described with reference to the following example.
An Iranian wax distillate having the following characteristics S. G. at F. 0.8775 Sulphur, wt. percent 1.52 Distillation Wt. percent 200 0-400 0. 13.1 Wt percent 400 C. 86.9
was passed over a catalyst consisting of cobalt molybdate supported on alumina at a temperature of about 780 F., at a pressure of 1000 lb.-/sq. in. and at a space velocity of 1.0 v./v./hr., together with hydrogen amounting to 4000 cu. ft. per barrel 3 of feedstock. The hydrofined product, after removal of the hydrogen sulphide, represented 97.2 wt. percent of the original feedstock and had the following characteristics:
S. G. at 140 F. 0.8445 Sulphur, wt. percent 0.04 Distillation:
Wt. percent to 200 C. 3.5 Wt. percent 200 C.-400 C 37.5 Wt percent 400 C. 59.0
The sulphur removed therefore amounted to 97.4% by wt. and it will be noted that there is considerably more material boiling within the range 200 C.-400 C.
The hydrofined product was then distilled for the recovery of a gas oil fraction representing 19% by weight on the original feedstock, the fraction having the characteristics set out in the following Table I:
Table I I. B.P C 213 10% C 247 50% C 307.5 F. B. P C Cut at 350 90% C 339.5 Sulphur content .048 Pour point F 30 Aniline point C 4'? Diesel index 33 The residue remaining after the separation of the gas oil fraction was then catalytically cracked in a fixed bed and the results of the cracking operation are set out in the following Table II with the results (for comparison) obtained by catalytically cracking the original feedstock.
Table II Rfesidue Original gg; feedstock Wax Dist Oat. cracking temperature, F 950 950 Feedrute g.l hr i 159. 155. 7 Products, wt. percent on Feed:
Gas 11.6 11. 2 Liquid 73. 1 79. 0 Carbon+Loss 15. 3 9. 8 Gasoline, wt. percent on fee 41. 1 32. 5 Gas Oil, wt. percent on iced l5. 6 22. 3 Inspection Date. on Gasoline to 430 F.:
S. G .7420 .7625 Total sulphur, wt. percent 0. 004 0. l4 Octane Number 80. l 77. 6 Wt. percent yield on original feedstock- 31. 4 32. 5 Inspection Date on Gas Oil, 430680 F.:
S. G. 00 F 0.9310 0. 9305 Sulphur, wt. percent. 0. 00 1. 70 Pour Point (upper) F 30 Carbon Residue (Con. 0.010 0. 3o Diesel Index 13 14 It will be seen from a consideration of Tables I and If, that the process of the invention has resulted in a yield amounting to 19% by wt. on the original feedstock of a gas oil fraction having a diesel index of 33 as compared with a cracked gas oil fraction having a diesel index of 14.
The yield of cracked gasoline based on the original feedstock has only fallen from 32.5% to 31.4% by weight on the original feedstock, while the octane number of the cracked gasoline has risen from 77.6 to 80.1.
We claim:
1. A process for the production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and. of a good quality diesel fuel without appreciable reduction in the maount of cracked gasoline which may be obtained from the wax distillate, which consists in passing the wax distillate to a hydrofining stage where it is contacted with a sulphurresistant hydrogenation catalyst in the presence of hydrogen and under conditions of temperature and pressure to effect the conversion of organically combined sulphur present in the feedstock into hydrogen sulphide, removing the hydrogen sulphide from the hydrofined feedstock, separating from the hydrofined feedstock a gas oil fraction suitable for use as a diesel fuel passing the residue boiling above the gas oil range to a catalytic cracking stage, and recovering gasoline from the cracked products.
2. A process for the production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate, which consists in passing the wax distillate to a hydrofining stage where it is contacted with a sulphur-resistant hydrogenation catalyst in the presence of hydrogen and under conditions of temperature and pressure to effect the conversion of organically combined sulphur present in the feedstock into hydrogen sulphide and to increase the content of material boiling within the range 200-400" (3., removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction boiling within the range ZOO-400 C. and suitable for use as a diesel fuel from the hydrofined feedstock passing the residue boiling above the gas oil range to a catalytic cracking stage, and recovering gasoline from the cracked products.
3. A process for the production from a sulphur-containing petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate, which consists in passing the wax distillate to a hydrofining stage where it is contacted with a catalyst of the cobalt molybdate type in the presence of hydrogen and under conditions of temperature and. pressure to effect conversion of organically combined sulfur present in the feedstock into hydrogen sulphide and to increase the amount of material boiling within the range 200-400 (3., removing the hydrogen sulphide from the hydrofined feedstock, separating a gas oil fraction boiling within the range 200-400 C. and suitable for use as a diesel fuel from the hydrofined feedstock, passing the residue boiling above the gas oil range to a catalytic cracking stage and separating from the catalytically cracked products a gasoline fraction of increased octane number and in substantially the same amount as would have been recovered from the products of catalytically cracking the feedstock without removal of said gas oil fraction.
4. A process for production from a sulphurcontaining petroleum feedstock boiling in the wax distillate range of cracked gasoline and of a good quality diesel fuel without appreciable reduction in the amount of cracked gasoline which may be obtained from the wax distillate, which consists in passing the wax distillate at the rate of 1.0 v./v./hr. to a hydrofining stage maintained at a temperature of about 780 F. and a pressure of 1000 lb./sq. in. together with hydrogen amounting to 4000 cu. ft. per barrel of feedstock,
we i to effect conversion of organically combined sulphur present in the feedstock into hydrogen sulphide and to increase the amount of material boiling within the range ZOO-400 0., removing the hydrogen sulphide from the hydrofined feedstock, separating from the hydrofined feedstock a gas oil fraction boiling within the range 200- 400 C. and suitable for use as a diesel fuel, the diesel index of said gas oil fraction being considerably higher than the diesel index of the corresponding fraction that can be recovered from the products of catalytically cracking the original feedstock, passing the residue boiling above the gas oil range to a catalytic cracking stage and recovering from the catalytically cracked products a gasoline fraction of increased octane number and in substantially the same amount as would have been recovered from the products of catalytically cracking the feedstock without removal of said gas oil fraction.
9 References Cited in the file of this patent UNITED STATES PATENTS Number Name Date ,282,451 Brooks May 12, 1942 2,291,885 Egloff Aug. 4, 1942 2,393,288 Byrns Jan. 22, 1946 2,417,308 Lee Mar. 11, 1947 2,541,229 Fleming Feb. 13, 1951 OTHER REFERENCES Production of Premium Diesel Fuels, by Geo. M. Woods (Part 1), page 99, Petroleum Engineer, November 1936.
Production of High Cetane Number Diesel Fuels by Hydrogenation, Tilton et al., presented before the Div. of Petroleum Chem, at the 111th meeting of the Amer. Chem. Soc., April 1947, Abs. P. 10-0.
Production of High Cetane Number Diesel Fuels by Hydrogenation, by Tilton et al., pages 1269 to 1273, Ind. and Eng. Chem., vol. 40, No. 7, July 1948.
Claims (1)
1. A PROCESS FOR THE PRODUCTION FROM A SULPHURCONTAINING PETROLEUM FEEDSTOCK BOILING IN THE WAX DISTILLATE RANGE OF CRACKED GASOLINE AND OF A GOOD QUALITY DIESEL FUEL WITHOUT APPRECIABLE REDUCTION IN THE AMOUNT OF CRACKED GASOLINE WHICH MAY BE OBTAINED FROM THE WAX DISTILLATE, WHICH CONSISTS IN PASSING THE WAX DISTILLATE TO A HYDROFINING STAGE WHERE IT IS CONTACTED WITH A SULPHURRESISTANT HYDROGENATION CATALYST IN THE PRESENCE OF HYDROGEN AND UNDER CONDITIONS OF TEMPERATURE AND PRESSURE TO EFFECT THE CONVERSION OF ORGANICALLY COMBINED SULPHUR PRESENT IN THE FEEDSTOCK INTO HYDROGEN SULPHIDE, REMOVING THE HYDROGEN SULPHIDE FROM THE HYDROFINED FEEDSTOCK, SEPARATING FROM THE HYDROFINED FEEDSTOCK A GAS OIL FRACTION SUITABLE FOR USE AS A DIESEL FUEL PASSING THE RESIDUE BOILING ABOVE THE GAS OIL RANGE TO A CATALYTIC CRACKING STAGE, AND RECOVERING GASOLINE FROM THE CRACKED PRODUCTS.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB2686150X | 1948-01-20 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2686150A true US2686150A (en) | 1954-08-10 |
Family
ID=10913446
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US70597A Expired - Lifetime US2686150A (en) | 1948-01-20 | 1949-01-12 | Catalytic cracking of petroleum hydrocarbons |
Country Status (1)
| Country | Link |
|---|---|
| US (1) | US2686150A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2775544A (en) * | 1955-02-28 | 1956-12-25 | Exxon Research Engineering Co | Production of catalytic cracking feed stocks |
| US2922759A (en) * | 1955-04-06 | 1960-01-26 | Texaco Inc | Hydrogenation process |
| US2924568A (en) * | 1955-02-28 | 1960-02-09 | Exxon Research Engineering Co | Process for hydrodesulfurizing and subsequently catalytically cracking gas oil |
| US3038843A (en) * | 1957-08-30 | 1962-06-12 | Union Oil Co | Distillation process and apparatus |
| US3503872A (en) * | 1968-02-02 | 1970-03-31 | Bethlehem Steel Corp | Hydrocracking of coal tar |
| US20090156876A1 (en) * | 2007-12-18 | 2009-06-18 | Ou John D Y | Apparatus and Process for Cracking Hydrocarbonaceous Feed Treated to Adsorb Paraffin-Insoluble Compounds |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2282451A (en) * | 1938-12-29 | 1942-05-12 | Standard Alcohol Co | Desulphurizing and cracking process |
| US2291885A (en) * | 1940-08-21 | 1942-08-04 | Universal Oil Prod Co | Catalytic conversion of hydrocarbons |
| US2393288A (en) * | 1943-07-06 | 1946-01-22 | Union Oil Co | Process for the catalytic reforming of hydrocarbon mixtures |
| US2417308A (en) * | 1943-04-12 | 1947-03-11 | Union Oil Co | Desulphurization and hydroforming |
| US2541229A (en) * | 1948-05-17 | 1951-02-13 | Phillips Petroleum Co | Catalytic hydrogenolysis of heavy residual oils |
-
1949
- 1949-01-12 US US70597A patent/US2686150A/en not_active Expired - Lifetime
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2282451A (en) * | 1938-12-29 | 1942-05-12 | Standard Alcohol Co | Desulphurizing and cracking process |
| US2291885A (en) * | 1940-08-21 | 1942-08-04 | Universal Oil Prod Co | Catalytic conversion of hydrocarbons |
| US2417308A (en) * | 1943-04-12 | 1947-03-11 | Union Oil Co | Desulphurization and hydroforming |
| US2393288A (en) * | 1943-07-06 | 1946-01-22 | Union Oil Co | Process for the catalytic reforming of hydrocarbon mixtures |
| US2541229A (en) * | 1948-05-17 | 1951-02-13 | Phillips Petroleum Co | Catalytic hydrogenolysis of heavy residual oils |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2775544A (en) * | 1955-02-28 | 1956-12-25 | Exxon Research Engineering Co | Production of catalytic cracking feed stocks |
| US2924568A (en) * | 1955-02-28 | 1960-02-09 | Exxon Research Engineering Co | Process for hydrodesulfurizing and subsequently catalytically cracking gas oil |
| US2922759A (en) * | 1955-04-06 | 1960-01-26 | Texaco Inc | Hydrogenation process |
| US3038843A (en) * | 1957-08-30 | 1962-06-12 | Union Oil Co | Distillation process and apparatus |
| US3503872A (en) * | 1968-02-02 | 1970-03-31 | Bethlehem Steel Corp | Hydrocracking of coal tar |
| US20090156876A1 (en) * | 2007-12-18 | 2009-06-18 | Ou John D Y | Apparatus and Process for Cracking Hydrocarbonaceous Feed Treated to Adsorb Paraffin-Insoluble Compounds |
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