US2967822A - Catalytic reforming of petroleum hydrocarbons with an alumina-chromium oxide catalyst comprising boron oxide - Google Patents
Catalytic reforming of petroleum hydrocarbons with an alumina-chromium oxide catalyst comprising boron oxide Download PDFInfo
- Publication number
- US2967822A US2967822A US700564A US70056457A US2967822A US 2967822 A US2967822 A US 2967822A US 700564 A US700564 A US 700564A US 70056457 A US70056457 A US 70056457A US 2967822 A US2967822 A US 2967822A
- Authority
- US
- United States
- Prior art keywords
- alumina
- oxide
- catalyst
- feedstock
- boron
- 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
- 239000003054 catalyst Substances 0.000 title claims description 20
- 229910000423 chromium oxide Inorganic materials 0.000 title claims description 10
- 239000003208 petroleum Substances 0.000 title description 6
- 238000001833 catalytic reforming Methods 0.000 title description 5
- 229930195733 hydrocarbon Natural products 0.000 title description 5
- 150000002430 hydrocarbons Chemical class 0.000 title description 5
- 229910052810 boron oxide Inorganic materials 0.000 title description 3
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 title description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 17
- WGLPBDUCMAPZCE-UHFFFAOYSA-N Trioxochromium Chemical compound O=[Cr](=O)=O WGLPBDUCMAPZCE-UHFFFAOYSA-N 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 8
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 claims description 7
- 229910052796 boron Inorganic materials 0.000 claims description 7
- 239000001257 hydrogen Substances 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical class [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 8
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- 238000009835 boiling Methods 0.000 description 6
- 238000002407 reforming Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 4
- 229910052697 platinum Inorganic materials 0.000 description 4
- 125000003118 aryl group Chemical group 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 150000002736 metal compounds Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- CHWRSCGUEQEHOH-UHFFFAOYSA-N potassium oxide Chemical compound [O-2].[K+].[K+] CHWRSCGUEQEHOH-UHFFFAOYSA-N 0.000 description 2
- 229910001950 potassium oxide Inorganic materials 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001339 alkali metal compounds Chemical class 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052792 caesium Inorganic materials 0.000 description 1
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910000420 cerium oxide Inorganic materials 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- QDOXWKRWXJOMAK-UHFFFAOYSA-N dichromium trioxide Chemical compound O=[Cr]O[Cr]=O QDOXWKRWXJOMAK-UHFFFAOYSA-N 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- MOWNZPNSYMGTMD-UHFFFAOYSA-N oxidoboron Chemical compound O=[B] MOWNZPNSYMGTMD-UHFFFAOYSA-N 0.000 description 1
- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 150000003112 potassium compounds Chemical class 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 229910052701 rubidium Inorganic materials 0.000 description 1
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-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
- C10G59/00—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha
- C10G59/02—Treatment of naphtha by two or more reforming processes only or by at least one reforming process and at least one process which does not substantially change the boiling range of the naphtha plural serial stages only
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
-
- 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
- C10G35/06—Catalytic reforming characterised by the catalyst used
Definitions
- This invention relates to the catalytic reforming of petroleum hydrocarbons for the production of aromatics, motor gasoline and the like.
- the object of the present invention is further to improve reforming processes using chromia-alumina catalyst.
- a feedstock consisting of or containing non-aromatic hydrocarbons is contacted with a catalyst comprising chromia, alumina and a minor proportion of boron, at a temperature of from 450 to 580 C. and a pressure up to 50 p.s.i.g. to yield a product with a higher aromatic content than the feedstock, there being no addition of hydrogen, whether extraneous or recycled, to the reaction zone.
- the present process besides yielding a normally liquid product having an appreciable content of aromatics and some olefins, also produces appreciable quantities of a hydrogen-rich gas, which is available as a valuable byproduct.
- a pressure up to 50 p.s.i.g. includes atmospheric pressure or below, atmospheric pressure being, in fact, preferred.
- a temperature in the vicinity of 525 C. is particularly preferred and the space velocity may be from 0.1 to 1.0 v./v./hr. of liquid feedstock.
- the boron in the catalyst is preferably present as an oxide and preferably there is also a minor proportion of an alkali metal compound, for example a potassium compound, particularly the oxide.
- the relative proportions of the catalyst components by weight of total catalyst material stable at 1020" F. are, preferably, within the limits:
- the catalyst may be used in the form of a fixed bed, a moving bed or a fluidized bed. Since it is readily regenerated by burning 01f carbonaceous deposits in a stream of oxygen-containing gas, it is particularly suitable for fluidized or moving bed processes.
- the process makes available a large quantity of hydrogen-rich gas as a valuable by-product.
- the feedstock used should boil within the gasoline or naphtha range, and a particularly preferred fraction consists predominantly of a mixture of C -C hydrocarbons.
- the feedstock may be a straight-run feedstock, particularly a lower-boiling straight-run fraction commonly known as primary flash distillate.
- gasoline blending components of high octane number and high volatility may be prepared from such feedstocks, in particular gasoline blending components having a research octane number (clear) of at least 90 and a volatility of at least 70%. evaporated at 100 C.
- the feedstock may be the product of a previous catalytic reforming process so that the present invention includes a two-stage reforming process designed to produce aromatics and high octane gasoline fractions with preferably a research octane number (clear) of the order of 100.
- a two-stage reforming process designed to produce aromatics and high octane gasoline fractions with preferably a research octane number (clear) of the order of 100.
- Any convenient reforming process may be used as the first stage, but
- the whole of the reformate from the first stage may be reformed in the second stage, but since the higher boiling end is rich in aromatics which are notsusceptible to further upgrading, the reformate is preferably fractionated to give a lower-boiling relatively aromatic-free fraction which is subjected to the further treatment.
- the reformate may be solvent extracted andthe raffinate or a fraction th'ereofsub jected to the further treatment.
- the product may be recombined with the higher boiling fraction or the solvent extract as the case may be, but it may also be combined with other high octane components for example heavy cat. cracked gasoline or alkylate.
- the catalyst may be prepared by any convenient method for example, by impregnation of alumina with a solution containing chromium, boron and preferably potassium.
- EXAMPLE 1 A platformate was split into light and heavy fractions, the light fraction having an end boiling point of 108 C. and a research octane number (clear) of 76.1. This light platformate was further reformed under the following conditions: a
- a process for the treatment of a feedstock consisting essentially of a mixture of C to C non-aromatic hydrocarbons to efiect a dehydrogenation or dehydrocyclization thereof comprising contacting the feedstock in a reaction zone with a catalyst consisting essentially of 5 to 25% of chromium oxide, 0.1 to 5% boron, expressed. as oxide, and balance, alumina, at a temperature of about 450 to 580 C., at a pressure not in excess of about p.s.i.g., at a space velocity of 0.1 to 1 v./v./ hr., and in the absence of added hydrogen to the reaction zone, and recovering a product having increased aromatic content.
- a process for the treatment of a feedstock consisting essentially of a mixture of C to C non-aromatic hydrocarbons to effect a dehydrogenation or dehydrocyclization thereof comprising contacting the feedstock in a reaction zone with a catalyst consisting essentially of 5 to 25% of chromium oxide, 0.1 to 5% boron, expressedas oxide, 0.1 to 5% of an alkali metal, expressed as oxide, and balance alumina, at a temperature of about 450. to 580 C., at a pressure not in excess of about 50 p.s.i.g., at a space velocity of 0.1 to 1 v./v./hr., and in the absence of added hydrogen to the reaction zone, and recovering a product having increased aromatic content.
- feedstock is a portion of a catalytic reformate, said portion consisting essentially of C to C non-aromatic hydrocarbons.
- feedstock is a portion of a platinum reformate, said portion consisting essentially of C to C non-aromatic hydrocarbons.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Description
United States Patent '0 CATALYTIC REFORMING F PETROLEUM HY- DROCARBONS WITH AN ALUMINA-CHROMIUM OXIDE CATALYST COMPRISING BORON OXIDE John Arthur Edgar Moy and Bernard Whiting Burbridge, Sunbury-on-Thames, England, assignors to The British Petroleum Company Limited, London, England, a British joint-stock corporation No Drawing. Filed Dec. 4, 1957, Ser. No. 700,564
Claims priority, application Great Britain Dec. 7, 1956 5 Claims. (Cl. 208-136) This invention relates to the catalytic reforming of petroleum hydrocarbons for the production of aromatics, motor gasoline and the like.
The catalytic reforming of petroleum hydrocarbons, for example naphtha fractions, to produce fractions of increased octane number is a well-known and established art. Various catalysts have been proposed as reforming catalysts; those most commonly employed comprise compounds of metals of group VI or group VIII of the periodic table on a support consisting of or containing aluminium oxide. Thus the conversion of aliphatic hydrocarbons to aromatic hydrocarbons has been described using a catalyst consisting of a minor proportion of chromium oxide supported on a major proportion of alumina. It has further been proposed to convert paraffinic and olefinic hydrocarbons in light petroleum fractions into aromatic hydrocarbons using a catalyst comprising a cyclizing metal compound such as chromium oxide sup ported on alumina and promoted with 2.5%-20% of a rare earth element and 6%30% of potassium or rubidium or caesium, both percentages being based on the weight of the cyclizing metal compound.
The object of the present invention is further to improve reforming processes using chromia-alumina catalyst.
According to the present invention, a feedstock consisting of or containing non-aromatic hydrocarbons is contacted with a catalyst comprising chromia, alumina and a minor proportion of boron, at a temperature of from 450 to 580 C. and a pressure up to 50 p.s.i.g. to yield a product with a higher aromatic content than the feedstock, there being no addition of hydrogen, whether extraneous or recycled, to the reaction zone.
The present process besides yielding a normally liquid product having an appreciable content of aromatics and some olefins, also produces appreciable quantities of a hydrogen-rich gas, which is available as a valuable byproduct. The term a pressure up to 50 p.s.i.g. includes atmospheric pressure or below, atmospheric pressure being, in fact, preferred. A temperature in the vicinity of 525 C. is particularly preferred and the space velocity may be from 0.1 to 1.0 v./v./hr. of liquid feedstock.
The boron in the catalyst is preferably present as an oxide and preferably there is also a minor proportion of an alkali metal compound, for example a potassium compound, particularly the oxide.
The relative proportions of the catalyst components by weight of total catalyst material stable at 1020" F., are, preferably, within the limits:
The catalyst may be used in the form of a fixed bed, a moving bed or a fluidized bed. Since it is readily regenerated by burning 01f carbonaceous deposits in a stream of oxygen-containing gas, it is particularly suitable for fluidized or moving bed processes.
The process makes available a large quantity of hydrogen-rich gas as a valuable by-product.
The feedstock used should boil within the gasoline or naphtha range, and a particularly preferred fraction consists predominantly of a mixture of C -C hydrocarbons. V
Thus according to one embodiment of the invention the feedstock may be a straight-run feedstock, particularly a lower-boiling straight-run fraction commonly known as primary flash distillate. By treatment according to the present invention gasoline blending components of high octane number and high volatility may be prepared from such feedstocks, in particular gasoline blending components having a research octane number (clear) of at least 90 and a volatility of at least 70%. evaporated at 100 C.
According to a further embodiment, the feedstock may be the product of a previous catalytic reforming process so that the present invention includes a two-stage reforming process designed to produce aromatics and high octane gasoline fractions with preferably a research octane number (clear) of the order of 100. Any convenient reforming process may be used as the first stage, but
those employing a catalyst of platinum on a support containing aluminium oxide. with or without halogen are preferred, such processes being hereinafter referred toas platinum reforming processes and the products as platinum reformates.
With a two-stage process, the whole of the reformate from the first stage may be reformed in the second stage, but since the higher boiling end is rich in aromatics which are notsusceptible to further upgrading, the reformate is preferably fractionated to give a lower-boiling relatively aromatic-free fraction which is subjected to the further treatment. Alternatively the reformate may be solvent extracted andthe raffinate or a fraction th'ereofsub jected to the further treatment. If desired, the product may be recombined with the higher boiling fraction or the solvent extract as the case may be, but it may also be combined with other high octane components for example heavy cat. cracked gasoline or alkylate.
The catalyst may be prepared by any convenient method for example, by impregnation of alumina with a solution containing chromium, boron and preferably potassium.
The invention is illustrated by the following examples:
EXAMPLE 1 A platformate was split into light and heavy fractions, the light fraction having an end boiling point of 108 C. and a research octane number (clear) of 76.1. This light platformate was further reformed under the following conditions: a
Four runs were carried out under these conditions using different catalysts as follows:
(1) 10% chromuim oxide on alumina.
(2) 10% chromium oxide on alumina with 1% cerium oxide and 1% potassium oxide.
(3) 10% chromium oxide on alumina with 1% boron on e.
(4) 10% chromium oxide on alumina with 1% boron oxide and 1% potassium oxide.
2,967,822 Patented Jan. 10, I961 3 All percentages are by weight of material stable at 1020 F. Comparative data for the four runs are shown in Table 1.
A light straight-run gasoline havingan ASTM boiling range of 41-87 C. and an octane number, research, clear, of 63.3 was treated under the followingprocess conditions:
Pressure Atmospheric Space velocity v./v./hr. 0.2 Recycle gas None Processing period ..hours 5 Runs were carried out at different temperatures using the catalysts of run 2 and run 4 of Example 1 respectively. The results are set out in Table 2 below.
Table 2 Debutanized Exit Gus Product Catalyst Temperature, C. Yield ON Flow H1001]..- (per- (Res) Rate, tent,
cent Clear s.c.f./b. percent wt.) vol.
475 86.1 82.0 853 32.7 a: as as ".2
87 cr'ce'KlAlumma We claim:
1. A process for the treatment of a feedstock consisting essentially of a mixture of C to C non-aromatic hydrocarbons to efiect a dehydrogenation or dehydrocyclization thereof comprising contacting the feedstock in a reaction zone with a catalyst consisting essentially of 5 to 25% of chromium oxide, 0.1 to 5% boron, expressed. as oxide, and balance, alumina, at a temperature of about 450 to 580 C., at a pressure not in excess of about p.s.i.g., at a space velocity of 0.1 to 1 v./v./ hr., and in the absence of added hydrogen to the reaction zone, and recovering a product having increased aromatic content.
2. A process for the treatment of a feedstock consisting essentially of a mixture of C to C non-aromatic hydrocarbons to effect a dehydrogenation or dehydrocyclization thereof comprising contacting the feedstock in a reaction zone with a catalyst consisting essentially of 5 to 25% of chromium oxide, 0.1 to 5% boron, expressedas oxide, 0.1 to 5% of an alkali metal, expressed as oxide, and balance alumina, at a temperature of about 450. to 580 C., at a pressure not in excess of about 50 p.s.i.g., at a space velocity of 0.1 to 1 v./v./hr., and in the absence of added hydrogen to the reaction zone, and recovering a product having increased aromatic content.
3. A process in accordance with claim 1, wherein the feedstock is a straight run distillate consisting of a mixture of C to C non-aromatic hydrocarbons.
4. A process in accordance with claim 1, wherein the feedstock is a portion of a catalytic reformate, said portion consisting essentially of C to C non-aromatic hydrocarbons.
5. A process in accordance with claim 1, wherein the feedstock is a portion of a platinum reformate, said portion consisting essentially of C to C non-aromatic hydrocarbons.
References Cited in the file of this patent UNITED STATES PATENTS 2,337,191 Greensfelder et a1 Dec. 21, 1943 2,404,024 Bailie et al July 16, 1946 2,409,695 Laughlin Oct. 22, 1946 2,656,304 MacPherson et al Oct. 20, 1953 2,697,684 Hemminger et al Dec. 21, 1954
Claims (1)
1. A PROCESS FOR THE TREATMENT OF A FEEDSTOCK CONSISTING ESSENTIALLY OF A MIXTURE OF C5 TO C7 NON-AROMATIC HYDROCARBONS TO EFFECT A DEHYDROGENATION OR DEHYDROCYCLIZATION THEREOF COMPRISING CONTACTING THE FEEDSTOCK IN A REACTION ZONE WITH A CATALYST CONSISTING ESSENTIALLY OF 5 TO 25% OF CHROMIUM OXIDE, 0.1 TO 5% BORON, EXPRESSED AS OXIDE, AND BALANCE ALUMINA, AT A TEMPERATURE OF ABOUT 450 TO 580*C., AT A PRESSURE NOT IN EXCESS OF ABOUT 50 P.S.I.G., AT A SPACE VELOCITY OF 0.1 TO 1 V./V./ HR., AND IN THE ABSENCE OF ADDED HYDROGEN TO THE REACTION ZONE, AND RECOVERING A PRODUCT HAVING INCREASED AROMATIC CONTENT.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB37463/56A GB827000A (en) | 1956-12-07 | 1956-12-07 | Improvements relating to the catalytic reforming of petroleum hydrocarbons |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2967822A true US2967822A (en) | 1961-01-10 |
Family
ID=10396674
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US700564A Expired - Lifetime US2967822A (en) | 1956-12-07 | 1957-12-04 | Catalytic reforming of petroleum hydrocarbons with an alumina-chromium oxide catalyst comprising boron oxide |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US2967822A (en) |
| BE (1) | BE568253A (en) |
| DE (1) | DE1054624B (en) |
| FR (1) | FR1187483A (en) |
| GB (1) | GB827000A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3230270A (en) * | 1960-08-18 | 1966-01-18 | Sinclair Research Inc | Alkylation of aromatics and catalyst therefor |
| US3243469A (en) * | 1962-08-10 | 1966-03-29 | Schneider Abraham | Production of 2, 6-dimethyl-naphthalene |
| US3417029A (en) * | 1963-04-05 | 1968-12-17 | Pullman Inc | Catalyst composition |
| US3472787A (en) * | 1968-01-19 | 1969-10-14 | Air Prod & Chem | Preparation of dried gel |
| US3871994A (en) * | 1970-10-09 | 1975-03-18 | Samuel J Tauster | Aromatization process |
| US4347123A (en) * | 1980-05-05 | 1982-08-31 | Exxon Research & Engineering Co. | Reforming with multimetallic catalysts |
| US4724226A (en) * | 1986-09-23 | 1988-02-09 | W. R. Grace & Co. | Boria-promoted HP catalyst |
| US20050011810A1 (en) * | 2003-07-18 | 2005-01-20 | Saudi Aramco | Catalytic naphtha reforming process |
| CN104209123A (en) * | 2014-08-11 | 2014-12-17 | 中国海洋石油总公司 | Light alkane dehydrogenation catalyst containing silver and boron and preparation method thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2337191A (en) * | 1942-12-07 | 1943-12-21 | Shell Dev | Dehydrogenation process |
| US2404024A (en) * | 1943-05-14 | 1946-07-16 | Standard Oil Co | Conversion catalyst |
| US2409695A (en) * | 1943-01-30 | 1946-10-22 | Standard Oil Dev Co | Method for improving aviation fuels |
| US2656304A (en) * | 1951-02-28 | 1953-10-20 | Standard Oil Dev Co | Continuous fluid hydroforming |
| US2697684A (en) * | 1951-11-28 | 1954-12-21 | Standard Oil Dev Co | Reforming of naphthas |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE855705C (en) * | 1943-05-21 | 1952-11-17 | Basf Ag | Process for the dehydrogenation and aromatization of hydrocarbons |
| DE814293C (en) * | 1949-05-19 | 1951-09-20 | Basf Ag | Process for carrying out catalytic reactions |
-
0
- BE BE568253D patent/BE568253A/xx unknown
-
1956
- 1956-12-07 GB GB37463/56A patent/GB827000A/en not_active Expired
-
1957
- 1957-12-04 US US700564A patent/US2967822A/en not_active Expired - Lifetime
- 1957-12-04 FR FR1187483D patent/FR1187483A/en not_active Expired
- 1957-12-06 DE DEB47027A patent/DE1054624B/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2337191A (en) * | 1942-12-07 | 1943-12-21 | Shell Dev | Dehydrogenation process |
| US2409695A (en) * | 1943-01-30 | 1946-10-22 | Standard Oil Dev Co | Method for improving aviation fuels |
| US2404024A (en) * | 1943-05-14 | 1946-07-16 | Standard Oil Co | Conversion catalyst |
| US2656304A (en) * | 1951-02-28 | 1953-10-20 | Standard Oil Dev Co | Continuous fluid hydroforming |
| US2697684A (en) * | 1951-11-28 | 1954-12-21 | Standard Oil Dev Co | Reforming of naphthas |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3230270A (en) * | 1960-08-18 | 1966-01-18 | Sinclair Research Inc | Alkylation of aromatics and catalyst therefor |
| US3243469A (en) * | 1962-08-10 | 1966-03-29 | Schneider Abraham | Production of 2, 6-dimethyl-naphthalene |
| US3417029A (en) * | 1963-04-05 | 1968-12-17 | Pullman Inc | Catalyst composition |
| US3472787A (en) * | 1968-01-19 | 1969-10-14 | Air Prod & Chem | Preparation of dried gel |
| US3871994A (en) * | 1970-10-09 | 1975-03-18 | Samuel J Tauster | Aromatization process |
| US4347123A (en) * | 1980-05-05 | 1982-08-31 | Exxon Research & Engineering Co. | Reforming with multimetallic catalysts |
| US4724226A (en) * | 1986-09-23 | 1988-02-09 | W. R. Grace & Co. | Boria-promoted HP catalyst |
| US20050011810A1 (en) * | 2003-07-18 | 2005-01-20 | Saudi Aramco | Catalytic naphtha reforming process |
| WO2005010128A1 (en) * | 2003-07-18 | 2005-02-03 | Saudi Arabian Oil Company | Catalytic naphtha reforming process |
| US7351325B2 (en) | 2003-07-18 | 2008-04-01 | Saudi Arabian Oil Company | Catalytic naphtha reforming process |
| US20080131338A1 (en) * | 2003-07-18 | 2008-06-05 | Saudi Arabian Oil Company | Catalytic naphtha reforming process |
| US7927556B2 (en) | 2003-07-18 | 2011-04-19 | Saudi Arabian Oil Company | Catalytic naphtha reforming process |
| CN104209123A (en) * | 2014-08-11 | 2014-12-17 | 中国海洋石油总公司 | Light alkane dehydrogenation catalyst containing silver and boron and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| GB827000A (en) | 1960-01-27 |
| FR1187483A (en) | 1959-09-11 |
| DE1054624B (en) | 1959-04-09 |
| BE568253A (en) |
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