US3072561A - Blocked hydrocarbon conversion operation permitting reduced tankage - Google Patents
Blocked hydrocarbon conversion operation permitting reduced tankage Download PDFInfo
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- US3072561A US3072561A US863014A US86301459A US3072561A US 3072561 A US3072561 A US 3072561A US 863014 A US863014 A US 863014A US 86301459 A US86301459 A US 86301459A US 3072561 A US3072561 A US 3072561A
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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
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
Definitions
- the present invention reduces tankage requirements. by feeding a heart cut continuously to the conversion process and blocking a light end or heavy end through the unit, and separately recovering the corresponding products.
- the tankage requirements for these ends are considerably less than in conventional systems.
- the present invention is particularly applicable to those situations where an overlap in the product characteristics is permissible. This invention can, however, be practiced in situations where it is desirable to separate the products obtained during each cycle of operation.
- the present invention comprises a process wherein hydrocarbons are converted by the alternate feeding to, and conversion in, a conversion zone a irst hydrocarbon stream and a second hydrocarbon stream, the initial boiling point of the second stream being at least 40 F. lower than the final boiling point of the rst stream.
- the improvement of this invention comprises separating a heart cut fraction from the two streams that boils within the range of the initial boiling point of the second stream and the nal boiling point of the first stream and continuously feeding this to the conversion zone while also alternately rfeeding the remainder of the rst stream or the remainder of the second stream to the conversion zone.
- the drawing schematically depicts a hydroforming process embodying the teachings of this invention. While the invention is described with refer ence to a naphtha hydroforming operation which usually operates on feeds boiling in the range of C4 to 430 F., it it applies equally as well to any one of several well known hydrocarbon conversion processes, such as steam cracking thermal cracking or reforming, gas oil catalytic ⁇ cracking, hydroiining, hydrodesulfurizing of naphthas, isomerizing and aromatizing, and the like.
- hydrocarbon conversion processes such as steam cracking thermal cracking or reforming, gas oil catalytic ⁇ cracking, hydroiining, hydrodesulfurizing of naphthas, isomerizing and aromatizing, and the like.
- the drawing illustrates a process for producing cornponents for a regular gasoline and a more volatile premium gasoline.
- the light feed is more severely treated to obtain a larger octane improvement, with smaller yields.
- Both the light and heavy products are passed to pools and blended to produce a regular and a premium gasoline.
- 2300 barrels per day of a regular gasoline are produced by blending, having a Research octane number of 92 with 1.5 cc. TEL/gal., an RVP of 12 p.s.i.g. when containing blended C4s (40% off at 158 F., 54% off at 212 and 95% off at 356).
- 2800 barrels per day of premium gasoline are produced by blending, having a Research octane number of 100 with 1.7 cc. TEL/gal., an RVP of l2 p.s.i.g. when containing 7% blended C4s (35% olf at 158 F., 54% off at 212 and 93% off at 320 R).
- the process equipment comprises a pipe still 1 or means for separating the feed, tanks 2 and 3 for alternately storing the blocked out feed, reforming system 4 and product storage tanks 5 and 6. Reforming system 3 has cycle.
- a Middle East crude is introduced into pipe still 1 by line 9 at a rate of 40,000 barrels per day. Material boiling below 160 F. and material boiling above 350 F. are removed and sent to further processing by lines 10 and 11, respectively.
- a 160/ 280 light cut and then a 280/ 350 heavy cut would alternately be introduced into the reforming system 4 from pipe still 1 on a 30 day cycle operating 6 days on heavy feed aud 24 days on light feed. This requires that 28,000 barrels of tankage be provided for the light cut and 28,000 barrels of tankage for the heavy cut.
- a 220/310 heart cut fraction is separated in the pipe still and continuously passed by line 12 to the reforming system when it is in operation.
- a 160/220 light ends fraction and a 310/350 heavy ends fraction are also separated and alternately Ifed to the reforming system along with the heart cut on a 30 day
- the heavy ends are passed to tankage, i.e. valve 13 is closed and valves 14, 15 and 16 are open.
- Light ends flow from the pipe still and feed tank A through lines 17 and 18, respectively, to line 12 and thence to the reforming system 4.
- valve 15 is closed and valves 14, 13 and 16 are open with the light ends flowing to feed tank A for storage.
- the heavy ends flow from pipe still 1 and from feed tank B by lines 19 ⁇ and 20,
- the light product can have a Research Clear octane number in the range of to 102 and boil in the range of 160 to 320 F., with a mid-boiling point in the range of 200 to 250 F.
- the heavy product can have a Research Clear octane number in the range of 70 to 100 and boil in the range of 200 to 430 F., with a mid-boiling point in the range of 250 to 350 F.
- Table 1 gives operating conditions for the portions A and B of the blocked operation and also gives a range of conditions for normal hydroforming operations.
- teachings of this invention can be followed by continuously feeding a 200/ 300 heart cut and alternately feeding a light C/200 cut and a heavy 300/ 430 cut.
- the two feeds may comprise a 350/500 fraction and a 430/650 fraction.
- a 430/500 heart cut fraction can be continuously fed to the process with a 350/ 430 fraction and a 500/ 650 fraction being blocked.
- a heart-cut fraction having a boiling range of about 200 to 300 F., a light ends fraction and a heavy ends fraction, alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the heavy ends fraction to storage and collecting the products of said first stream conversion, and then combining the heavy ends fraction with the heart-cut fraction to form said second stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion, wherein said conversion zone contains a reforming catalyst and operates at an average ternperature in the range of 850 to 1000 F., a pressure in the range of 250 to 650 p.s.i.a., a feed rate in the range of 0.4 to 3 w./h./w.
- said first product has a Research Clear octane number in the range of 90 to 102, boils in the range of 160 to 320 F., with a midboiling point in the range of 200 to 250 F.
- said second product has a Research Clear octane number in the range of 70 to 100, and boils in the range of 200 to 430 F., with a mid-boiling point in the range of 250 to 350 F.
- the improvement which comprises fractionating a wide boiling range feed to separate the same into a heart-cut fraction having a boiling range of at least 40 F., a light ends fraction and a heavy ends fraction, alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the heavy ends fraction to storage, and collecting the products of said first stream conversion and then combining the heavy ends fraction with the heart-cut fraction to form said second stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion.
- a heart-cut fraction having a boiling range of about 200 to 300 F.
- a light ends fraction and a heavy ends fraction alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to a catalytic hydroforming reaction conversion zone, wherein free hydrogen containing gas is also introduced into said zone, while simultaneously passing the heavy ends fraction to storage, and collecting the products of said first stream conversion and then combining the heavy ends fraction with the heart-cut fraction to form said second stream and charging the same to said conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion.
- the improvement which comprises fractionating a hydrocarbon stream boiling in the range of about C5 to 430 F. to separate the same into a heart-cut fraction having a boiling range of about 200 to 300 lF., a light ends fraction having a boiling range of about C5 to 200 F. and a heavy ends fraction having a boiling range of about 300 to 430 F. alternately combining the light ends fraction with the heart cut fraction to form said first stream having a boiling range of about C5 to 300 F.
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
PERMITTING REDUCED TANKAGE Filed D60. 30, 1959 Jan. 8, 1963 Inventor Robert P. Cahn Patent Attorney United States Patent Olice 3,072,561 BLOCKED HYDROCARBON CONVERSION OPERA- TION PERMITTING REDUCED TANKAGE Robert P. Cahn, Elizabeth, NJ., assignor t Esso Research and Engineering Company, a corporation of Delaware Filed Dec. 30, 1959, Ser. No. 863,014 Claims. (Cl. 208-80) This invention is concerned with a blocked operation wherein two hydrocarbon streams of different boiling ranges are alternately fed to a conversion process to produce two types of products. The heart cut blocked operation of the presen-t invention permits considerable savings in tankage investments.
The present invention reduces tankage requirements. by feeding a heart cut continuously to the conversion process and blocking a light end or heavy end through the unit, and separately recovering the corresponding products. The tankage requirements for these ends are considerably less than in conventional systems. The present invention is particularly applicable to those situations where an overlap in the product characteristics is permissible. This invention can, however, be practiced in situations where it is desirable to separate the products obtained during each cycle of operation.
In brief compass, the present invention comprises a process wherein hydrocarbons are converted by the alternate feeding to, and conversion in, a conversion zone a irst hydrocarbon stream and a second hydrocarbon stream, the initial boiling point of the second stream being at least 40 F. lower than the final boiling point of the rst stream. The improvement of this invention comprises separating a heart cut fraction from the two streams that boils within the range of the initial boiling point of the second stream and the nal boiling point of the first stream and continuously feeding this to the conversion zone while also alternately rfeeding the remainder of the rst stream or the remainder of the second stream to the conversion zone.
The following description of the drawing attached to and forming a part of this specification will serve to make this invention clear. The drawing schematically depicts a hydroforming process embodying the teachings of this invention. While the invention is described with refer ence to a naphtha hydroforming operation which usually operates on feeds boiling in the range of C4 to 430 F., it it applies equally as well to any one of several well known hydrocarbon conversion processes, such as steam cracking thermal cracking or reforming, gas oil catalytic` cracking, hydroiining, hydrodesulfurizing of naphthas, isomerizing and aromatizing, and the like.
The drawing illustrates a process for producing cornponents for a regular gasoline and a more volatile premium gasoline. The light feed is more severely treated to obtain a larger octane improvement, with smaller yields. Both the light and heavy products are passed to pools and blended to produce a regular and a premium gasoline. 2300 barrels per day of a regular gasoline are produced by blending, having a Research octane number of 92 with 1.5 cc. TEL/gal., an RVP of 12 p.s.i.g. when containing blended C4s (40% off at 158 F., 54% off at 212 and 95% off at 356). 2800 barrels per day of premium gasoline are produced by blending, having a Research octane number of 100 with 1.7 cc. TEL/gal., an RVP of l2 p.s.i.g. when containing 7% blended C4s (35% olf at 158 F., 54% off at 212 and 93% off at 320 R).
The process equipment comprises a pipe still 1 or means for separating the feed, tanks 2 and 3 for alternately storing the blocked out feed, reforming system 4 and product storage tanks 5 and 6. Reforming system 3 has cycle.
a design capacity of 5800 barrels per day and contains a totalof 80 tons of 0.6 wt. percent platinum on eta alumina catalyst. It is operated in a semi-regenerative fashion with four reactors. The unit is shut down for regeneration every 2-3 months. Hydrogen produced in the process is removed by line 7 and a portion thereof is recycled by line 8 as is necessary.
A Middle East crude is introduced into pipe still 1 by line 9 at a rate of 40,000 barrels per day. Material boiling below 160 F. and material boiling above 350 F. are removed and sent to further processing by lines 10 and 11, respectively.
In a normal blocked operation, a 160/ 280 light cut and then a 280/ 350 heavy cut would alternately be introduced into the reforming system 4 from pipe still 1 on a 30 day cycle operating 6 days on heavy feed aud 24 days on light feed. This requires that 28,000 barrels of tankage be provided for the light cut and 28,000 barrels of tankage for the heavy cut.
In the present invention, a 220/310 heart cut fraction is separated in the pipe still and continuously passed by line 12 to the reforming system when it is in operation. A 160/220 light ends fraction and a 310/350 heavy ends fraction are also separated and alternately Ifed to the reforming system along with the heart cut on a 30 day During operation A, that part of the cycle when the light ends are fed, the heavy ends are passed to tankage, i.e. valve 13 is closed and valves 14, 15 and 16 are open. Light ends flow from the pipe still and feed tank A through lines 17 and 18, respectively, to line 12 and thence to the reforming system 4. During operation B when the heavy ends are being fed, valve 15 is closed and valves 14, 13 and 16 are open with the light ends flowing to feed tank A for storage. The heavy ends flow from pipe still 1 and from feed tank B by lines 19` and 20,
respectively, to line 12 and thence to the reforming sysem.
During operation B the regular gasoline is passed from the reforming system by lines 21 and 22 to product tank B with Valve 24 being closed. During A operation the premium gasoline is collected in product tank A with valve 24 being open and valve 23 being closed. The system illustrated requires that feed tank A have a cap actiy of only 14,000 barrels and feed tank B a capacity of only 16,000 barrels.
It can be appreciated that the two products from the hydroformer have different essential characteristics. The light product can have a Research Clear octane number in the range of to 102 and boil in the range of 160 to 320 F., with a mid-boiling point in the range of 200 to 250 F. The heavy product can have a Research Clear octane number in the range of 70 to 100 and boil in the range of 200 to 430 F., with a mid-boiling point in the range of 250 to 350 F.
Table 1 gives operating conditions for the portions A and B of the blocked operation and also gives a range of conditions for normal hydroforming operations.
In a steam cracking operation one may wish to a1- ternately feed a C5/ 300 feed and then -a 200/4,30 feed.
Patented Jan. 8, 1963 In this case, the teachings of this invention can be followed by continuously feeding a 200/ 300 heart cut and alternately feeding a light C/200 cut and a heavy 300/ 430 cut. In a hydroning process the two feeds may comprise a 350/500 fraction and a 430/650 fraction. Thus, in accordance with this invention a 430/500 heart cut fraction can be continuously fed to the process with a 350/ 430 fraction and a 500/ 650 fraction being blocked.
Having described this invention, what is sought to be protected by Letters Patent is succinctly set forth in the following claims.
What is claimed is:
1. In a process wherein hydrocarbons are converted by the alternate feeding to and conversion in a conversion zone of a first stream and a second stream of hydrocarbons, the initial boiling point of said second stream being at least 40 F. lower than the final boiling point of said first stream wherein a free hydrogen containing gas is also introduced into said conversion Zone, the improvement which comprises fractionating a naphtha boiling in the range of about C4 to 430 F. to separate the same into a heart-cut fraction having a boiling range of about 200 to 300 F., a light ends fraction and a heavy ends fraction, alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the heavy ends fraction to storage and collecting the products of said first stream conversion, and then combining the heavy ends fraction with the heart-cut fraction to form said second stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion, wherein said conversion zone contains a reforming catalyst and operates at an average ternperature in the range of 850 to 1000 F., a pressure in the range of 250 to 650 p.s.i.a., a feed rate in the range of 0.4 to 3 w./h./w. and a hydrogen partial pressure in the range of 200 to 400 p.s.i., and wherein said first product has a Research Clear octane number in the range of 90 to 102, boils in the range of 160 to 320 F., with a midboiling point in the range of 200 to 250 F., and wherein said second product has a Research Clear octane number in the range of 70 to 100, and boils in the range of 200 to 430 F., with a mid-boiling point in the range of 250 to 350 F.
2. In a process wherein hydrocarbons are converted by the alternate feeding to and conversion in a conversion Zone of a lirst stream and a second stream of hydrocarbons, the initial boiling point of said second stream being at least 40 F. lower than the final boiling point of said first stream, the improvement which comprises fractionating a wide boiling range feed to separate the same into a heart-cut fraction having a boiling range of at least 40 F., a light ends fraction and a heavy ends fraction, alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the heavy ends fraction to storage, and collecting the products of said first stream conversion and then combining the heavy ends fraction with the hart-cut fraction to form said second stream and charging the same to the hydrocarbon conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion.
3. In a process wherein hydrocarbons are converted by the alternate feeding to and conversion in a conversion zone of a first stream and a second stream of hydrocarbons, the initial boiling point of said second stream being at least 40 F. lower than the final boiling point of said first stream, the improvement which comprises fractionating a naphtha boiling in the range of abou't C4 to 430 F. to separate the same in to a heart-cut fraction having a boiling range of about 200 to 300 F., a light ends fraction and a heavy ends fraction, alternately combining the light ends fraction with the heart-cut fraction to form said first stream and charging the same to a catalytic hydroforming reaction conversion zone, wherein free hydrogen containing gas is also introduced into said zone, while simultaneously passing the heavy ends fraction to storage, and collecting the products of said first stream conversion and then combining the heavy ends fraction with the heart-cut fraction to form said second stream and charging the same to said conversion zone while simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion.
5. In a process wherein hydrocarbons are converted by hydroiining by the alternate feeding to and conversion in a conversion Zone of a iirst stream and a second stream of hydrocarbons, the initial boiling point of said second stream being at least 40 F. lower than the final boiling point of said iirst stream, the improvement which comprises fractionating a hydrocarbon stream boiling in the range of about 350 to 650 F. to separate the same into a heart-cut fraction having a boiling range of about 430 to 500 F., a light ends fraction having a boiling range of about 350 to 430 F. and a heavy ends fraction boiling in the range of about 500 to 650 F. alternately cornbining the light ends fraction with the heart-cut fraction to form said first stream boiling in the range of about 350 to 500 F. and charging the same to the hydrocarbon conversion zone while simultaneously passing the heavy ends fraction to storage, and collecting the products of said first stream conversion and then combining the heavy ends fraction with the heart-cut fraction to form said second stream boiling in the range of about 430 to 650, and charging the same to the hydrocarbon conversion zone While simultaneously passing the light ends fraction to storage and collecting the products from said second stream conversion.
References Cite in the tile of this patent UNITED STATES PATENTS 2,067,030 Van Peski Ian. 5, 1937 2,249,461 Diwoky July l5, 1941 2,255,399 Subkow et al. Sept. 9, 1941 2,335,684V Mayer Nov. 30, 1943 2,636,909 Oblad Apr. 28, 1953 3,002,917 Hamilton Oct. 3, 1961
Claims (1)
1. IN A PROCESS WHEREIN HYDROCARBONS ARE CONVERTED BY THE ALTERNATE FEEDING TO AND CONVERSION IN A CONVERSION ZONE OF A FIRST STREAM AND A SECOND STREAM OF HYDROCARBONS, THE INITIAL BOILING POINT OF SAID SECOND STREAM BEING AT LEAST 40*F. LOWER THAN THE FINAL BOILING POINT OF SAID FIRST STREAM WHEREIN A FREE HYDROGEN CONTAINING GAS IS ALSO INTRODUCED INTO SAID CONVERSION ZONE, THE IMPROVEMENT WHICH COMPRISES FRACTIONATING A NAPHTHA BOILING IN THE RANGE OF ABOUT C4 TO 430*F. TO SEPARATE THE SAME INTO A HEART-CUT FRACTION HAVING A BOILING RANGE OF ABOUT 200 TO 300*F., A LIGHT ENDS FRACTION AND A HEAVY ENDS FRACTION, ALTERNATELY COMBINING THE LIGHT ENDS FRACTION WITH THE HEART-CUT FRACTION TO FORM SAID FIRST STREAM AND CHARGING THE SAME TO THE HYDROCARBON CONVERSION ZONE WHILE SIMULTANEOUSLY PASSING THE HEAVY ENDS FRACTION TO STORAGE AND COLLECTING THE PRODUCTS OF SAID FIRST STREAM CONVERSION, AND THEN COMBINING THE HEAVY ENDS FRACTION WITH THE HEART-CUT FRACTION TO FORM SAID SECOND STREAM AND CHARGING THE SAME TO THE HYDROCARBON CONVERSION
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US863014A US3072561A (en) | 1959-12-30 | 1959-12-30 | Blocked hydrocarbon conversion operation permitting reduced tankage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US863014A US3072561A (en) | 1959-12-30 | 1959-12-30 | Blocked hydrocarbon conversion operation permitting reduced tankage |
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| US3072561A true US3072561A (en) | 1963-01-08 |
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| US863014A Expired - Lifetime US3072561A (en) | 1959-12-30 | 1959-12-30 | Blocked hydrocarbon conversion operation permitting reduced tankage |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3305476A (en) * | 1964-12-14 | 1967-02-21 | Standard Oil Co | Balanced-octane gasoline manufacture |
| US3456031A (en) * | 1968-07-05 | 1969-07-15 | Universal Oil Prod Co | Selective catalytic dehydrogenation of a mixture of normal paraffin hydrocarbons |
| US3472761A (en) * | 1967-03-28 | 1969-10-14 | Continental Oil Co | Process for the manufacture of two or more grades of petroleum coke |
| US3474156A (en) * | 1968-04-03 | 1969-10-21 | Universal Oil Prod Co | Selective catalyst dehydrogenation of a mixture of normal paraffin hydrocarbons |
| FR2372884A1 (en) * | 1976-12-03 | 1978-06-30 | Chevron Res | "ALTERNATE" REFORMATION AND ISOMERIZATION PROCESS |
| US20080194901A1 (en) * | 2004-12-23 | 2008-08-14 | Michiel Cramwinckel | Process To Prepare Two Iso Paraffinic Products From A Fischer-Tropsch Derived Feed |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US206700A (en) * | 1878-08-06 | Improvement in wire-rope ways | ||
| US2249461A (en) * | 1937-08-17 | 1941-07-15 | Standard Oil Co | Manufacture of antiknock gasoline |
| US2255399A (en) * | 1935-10-29 | 1941-09-09 | Union Oil Co | Process for cracking and polymerizing hydrocarbons |
| US2335684A (en) * | 1943-11-30 | Catalytic reforming | ||
| US2636909A (en) * | 1953-04-28 | Production of akomatic | ||
| US3002917A (en) * | 1959-10-01 | 1961-10-03 | Socony Mobil Oil Co Inc | Method of making 104-106 r.o.n. leaded gasoline |
-
1959
- 1959-12-30 US US863014A patent/US3072561A/en not_active Expired - Lifetime
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US206700A (en) * | 1878-08-06 | Improvement in wire-rope ways | ||
| US2335684A (en) * | 1943-11-30 | Catalytic reforming | ||
| US2636909A (en) * | 1953-04-28 | Production of akomatic | ||
| US2255399A (en) * | 1935-10-29 | 1941-09-09 | Union Oil Co | Process for cracking and polymerizing hydrocarbons |
| US2249461A (en) * | 1937-08-17 | 1941-07-15 | Standard Oil Co | Manufacture of antiknock gasoline |
| US3002917A (en) * | 1959-10-01 | 1961-10-03 | Socony Mobil Oil Co Inc | Method of making 104-106 r.o.n. leaded gasoline |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3305476A (en) * | 1964-12-14 | 1967-02-21 | Standard Oil Co | Balanced-octane gasoline manufacture |
| US3472761A (en) * | 1967-03-28 | 1969-10-14 | Continental Oil Co | Process for the manufacture of two or more grades of petroleum coke |
| US3474156A (en) * | 1968-04-03 | 1969-10-21 | Universal Oil Prod Co | Selective catalyst dehydrogenation of a mixture of normal paraffin hydrocarbons |
| US3456031A (en) * | 1968-07-05 | 1969-07-15 | Universal Oil Prod Co | Selective catalytic dehydrogenation of a mixture of normal paraffin hydrocarbons |
| FR2372884A1 (en) * | 1976-12-03 | 1978-06-30 | Chevron Res | "ALTERNATE" REFORMATION AND ISOMERIZATION PROCESS |
| US20080194901A1 (en) * | 2004-12-23 | 2008-08-14 | Michiel Cramwinckel | Process To Prepare Two Iso Paraffinic Products From A Fischer-Tropsch Derived Feed |
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