GB2087747A - Improvements in or relating to a hydrotreating catalyst - Google Patents
Improvements in or relating to a hydrotreating catalyst Download PDFInfo
- Publication number
- GB2087747A GB2087747A GB8135076A GB8135076A GB2087747A GB 2087747 A GB2087747 A GB 2087747A GB 8135076 A GB8135076 A GB 8135076A GB 8135076 A GB8135076 A GB 8135076A GB 2087747 A GB2087747 A GB 2087747A
- Authority
- GB
- United Kingdom
- Prior art keywords
- catalyst
- hydrotreating
- diameter
- pores
- catalyst according
- 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.)
- Granted
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 59
- 239000011148 porous material Substances 0.000 claims abstract description 23
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims abstract description 20
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000001354 calcination Methods 0.000 claims abstract description 11
- 229910052759 nickel Inorganic materials 0.000 claims abstract description 10
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims abstract description 9
- 229910052750 molybdenum Inorganic materials 0.000 claims abstract description 9
- 239000011733 molybdenum Substances 0.000 claims abstract description 9
- 238000009835 boiling Methods 0.000 claims abstract description 7
- 229910017052 cobalt Inorganic materials 0.000 claims description 7
- 239000010941 cobalt Substances 0.000 claims description 7
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000003079 shale oil Substances 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 101100123850 Caenorhabditis elegans her-1 gene Proteins 0.000 description 1
- APUPEJJSWDHEBO-UHFFFAOYSA-P ammonium molybdate Chemical compound [NH4+].[NH4+].[O-][Mo]([O-])(=O)=O APUPEJJSWDHEBO-UHFFFAOYSA-P 0.000 description 1
- 229940010552 ammonium molybdate Drugs 0.000 description 1
- 235000018660 ammonium molybdate Nutrition 0.000 description 1
- 239000011609 ammonium molybdate Substances 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000007788 liquid Substances 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
- 239000005078 molybdenum compound Substances 0.000 description 1
- 150000002752 molybdenum compounds Chemical class 0.000 description 1
- KBJMLQFLOWQJNF-UHFFFAOYSA-N nickel(ii) nitrate Chemical compound [Ni+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O KBJMLQFLOWQJNF-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000011295 pitch Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001694 spray drying Methods 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000005292 vacuum distillation Methods 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
- C10G49/00—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00
- C10G49/02—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used
- C10G49/04—Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups C10G45/02, C10G45/32, C10G45/44, C10G45/58 or C10G47/00 characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/61—Surface area
- B01J35/615—100-500 m2/g
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/63—Pore volume
- B01J35/635—0.5-1.0 ml/g
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/64—Pore diameter
- B01J35/647—2-50 nm
-
- 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
- B01J35/00—Catalysts, in general, characterised by their form or physical properties
- B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
- B01J35/64—Pore diameter
- B01J35/651—50-500 nm
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Materials Engineering (AREA)
- Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
A catalyst, for hydrotreating heavy feedstocks, comprised of nickel and molybdenum supported on alumina having a defined pore size distribution which has been calcined at a temperature of from 621 DEG C to 705 DEG C, and a process for hydrotreating using the catalyst. Calcining of such a catalyst at such temperatures has been found to provide for effective use thereof as a hydrotreating catalyst for higher boiling feedstocks.
Description
SPECIFICATION
Improvements in or relating to a hydrotreating catalyst
This invention relates to a hydrotreating catalyst and to a process using the catalyst.
In the hydrotreating of a hydrocarbon-containing feedstock, the hydrotreating is generally accomplished in the presence of a hydrotreating catalyst comprising Group VI and Group VII metals supported on a suitable support. There is a continued need for improvements in such catalysts to provide improved activity and longer catalyst life.
Accordingly, one aspect of the present invention provides a hydrotreating catalyst comprising: a catalytically effective amount of nickel and molybdenum supported on an alumina support, the catalyst having a total porosity of at least 0.5 cc/g and a pore size distribution of from 0.25 to 0.40 cc/g of pores with a diameter of less than 25 nm, from 0.10 to 0.25 cc/g of pores with a diameter of from 25 to 50 nm, from 0.20 to 0.30 cc/g of pores with a diameter of from 50 to 150 nm, from 0.05 to 0.15 cc/g of pores with a diameter of from 150 to 400 nm, and from 0.03 to 0.10 cc/g of pores with a diameter of greater than 400 nm, the catalyst having been prepared with calcining at a temperture of from 621"C to 705"C.
The inventor has found that calcining of the catalyst at temperatures normally used for the calcining of supported nickel-containing catalysts (about 1000 - 1050"F (537 to 565or)) does not provide a usable catalyst for the hydrotreating of higher boiling feedstocks because severe coking of the catalyst occurs after only a short period of opertion.
The catalyst in accordance with the invention may further include cobalt. Preferably, the catalyst contains from 1% to 6% (preferably from 1% to 4%) of nickel; from 5% to 16% (preferably from 6% to 10%) of molybdenum; and 0% to 6% of cobalt, all by weight. If cobalt is employed, the cobalt is most preferably present in an amount of from 1% to 6% by weight
The particle size of a catalyst in accordance with the invention is preferably from 0.005 to 0.125 inch (12.7 to 31.8 mm) (if the catalyst is in spherical form) orfrom 0.015 to 0.125 inch (38.1 to 317.5 mm) if the catalyst is in extruded form.
Advantageously, the surface area of the catalyts is at least 125 m2/g, and most advantageously from 150 300 m2/g. The alumina of the catalyst is preferably the gamma form thereof. In some cases, the alumina support includes up to 10% of silica.
The nickel and molybdenum and cobalt, if present, are supported on the alumina by procedures generally known in the art. Thus, for example, a molybdenum compound such as ammonium molybdate may be added to an aqueous slurry of the alumina having a porosity and pore size distribution to provide a finished catalyst having the hereinabove-defined porosity and pore size distribution, followed by spray drying and formation into, for example, spheres. The supported molybdenum may be calcined at this time; however, such calcining would be additional to and not in lieu of the final calcination in accordance with the invention.
The molybdenum supported on the alumina is then impregnated with nickel, for example as aqueous nickel nitrate, and optionally also cobalt, followed by drying.
The supported catalyst is then calcined in accordance with the invention at a temperature of from 11 500F to 1300"F (621to 705"C), preferably from 1150"F to 1250"F (621"C to 6770C) and most preferably about 1 200"F (649"C). As hereinabove noted the use of lower calcination temperatures, as conventionally employed for supported catalysts containing nickel, does not provide an acceptable catalyst (because of excessive coke lay-down), and temperatures above 1300"F (705"C) would not be suitable because of molybdenum volatility.
In using the higher of the disclosed calcining temperatures there may be some deactivation of the nickel component of the catalyst, and as a result, in most cases the calcination temperature should not exceed 12500F (6770C).
A second aspect of the invention provides a process for the catalytic hydrotreating of a hydrocarboncontaining feedstock in the presence of a hydrotreating catalyst in accordance with the first aspect of the invention.
The said hydrocarbon-containing feedstocks preferably contain heavier (higher boiling) components.
Such feedstocks are most preferably those in which at least 50% of the components boil above 975"F (533"C) and are conveniently derived from either petroleum or coal sources. Representative examples of such feedstocks include: heavy petroleum crudes, petroleum residues from atmospheric or vacuum distillations, shale oil, shale oil residues, tar sands, bitumen, coal tar pitches, solvent refined coal and solvent deasphalted oils.
The hydrotreating of the feedstock is accomplished at conditions which are generally known in the art to be effective for upgrading the feedstock. The catalyst is preferably presulphided. Preferably, the hydrotreating is accomplished at from 700O to 9000F (371"C to 483 C), most preferably from 750O to 850"F (398"C to 455"C) and at from 1000 to 3500 psig (6.895 kN/m2 to 241.3 kN/m2g), preferably from 1500 to 3000 psig (10.34 kN/m2 to 20.69 kN/m2g).The liquid hourly space velocity is generally of the order of from 0.05 to 2.0 her1, preferably 0.1 to 1.0 hr1.The hydrogen is supplied in an amount sufficient to accomplish the hydrotreating, with such hydrogen preferably being employed in an amount of from 2000 to 6000 SCF/bbl. of feed (14953 m3/m3 to 44861 m3/m3), most preferably from 4000 to 5000 SCF/bbl (29907 to 37384 m3/m3 of feed). Gas volumes in this specification are taken to be at s.t.p. (00C, 1 atm).
The hydrotreating may be effected in any one of a wide variety of reactors, for example a fixed bed reactor, a moving bed reactor, a fluidized bed reactor, or an expanded bed reactor, any one of which may contain one or more beds of the catalyst.
As known in the art, such hydrotreating upgrades the feedstock by conversion of higher boiling components to lower boiling components. In addition, desulphurization and/or denitrogenation is also accomplished.
The invention will be further described with respect to the following Example:
Example
A catalyst was prepared which comprised 12.0% MoO3,1.5% CoO and 1.5% NiO supported on gamma-alumina having a total porosity of 0.87 - 0.89% cc/g and a pore size distribution as follows:
Pore Diameter, nm Porosity, cclg 25 0.34-0.36
25-50 0.14-0.15 50 - 150 0.22-0.23
150-400 0.10-0.11
400 0.04-0.07
The catalyst was in the form of spheres having a diameter of the order of 0.015 to 0.0.035 inch (38.1 to 88.9 mm).
In one case (case A) the catalyst was calcined at 1050"F (565.5"C) and in the other case (case B) the catalyst was calcined in accordance with the invention at 1 2000F (649"C).
Each of the catalysts was presulphided in the reactor and tested for the hydrotreating of Cold Lake
Atmospheric Residue, as an ebullated catalyst bed, at 730"F (388"C) and at a hydrogen pressure of 2000 psig (13.79 kN/m2g), with hydrogen being used at a rate of 5000 SCF/bbl of feed (37384 m3/m3 of feed).
The case A catalyst coked up within 24 hours.
The case B catalyst in accordance with the invention operated for 35 days with the temperature eventually being raised to 8200F (438"C). The conversion rate was of the order of 60%, based on the 975"F+ (524"C+) components of the feed.
Thus, catalysts in accordance with the present invention have been found to be effective for upgrading heavier hydrocarbon feedstocks and have been found to be capable of operating over long periods of time and at conversion rates of 40% or greater (in most cases in excess of 50% and even of the order of 60%) based on the 975 F+ (524 C+) components of the feed.
Claims (16)
1. A hydrotreating catalyst comprising: a catalytically effective amount of nickel and molybdenum supported on an alumina support, the catalyst having a total porosity of at least 0.5 cc/g and a pore size distribution of from 0.25 to 0.40 cc/g of pores with a diameter of less than 25 nm, from 0.10 to 0.25 cc/g of pores with a diameter of from 25 to 50 nm, from 0.20 to 0.30 cc/g of pores with a diameter of from 50 to 150 nm, from 0.05 to 0.15 cc/g of pores with a diameter of from 150 to 400 nm, and from 0.03 to 0.10 cc/g of pores with a diameter of greater than 400 nm, the catalyst having been prepared with calcining at a temperature of from 621"C to 705"C.
2. A catalyst according to claim 1, wherein the specific surface area of the catalyst is at least 1 25m2/g.
3. A catalyst according to claim 2, wherein the specific surface area of the catalyst is from 150 - 300 m2/g.
4. A catalyst according to any one of the preceding claims, wherein the pore distribution is: from 0.34 to 0.36 cclg of pores of a diameter of less than 25 nm, from 0.14 to 0.15 cc/g of pores with a diameter of from 25 to 50 nm, from 0.22 to 0.23 cc/g of pores with a diameter of from 50 - 150 nm, from 0.10 to 0.11 cc/g of pores having a diameter of from 150 to 400 nm, and from 0.04 to 0.07 cc/g of pores with a diameter of greater than 400 nm.
5. A catalyst according to any one of the preceding claims, wherein the catalyst comprises from 1 % to 6% of nickel and from 5% to 16% of molybdenum, by weight.
6. A catalyst according to any one of the preceding claims, wherein the said temperature of calcining is from 621"C to 677"C.
7. A catalyst according to any one of the preceding claims, wherein the total porosity is from 0.75 to 0.95 cc/g.
8. A catalyst according to any one of the preceding claims, wherein the alumina is gamma-alumina.
9. A catalyst according to any one of the preceding claims, wherein the catalyst further comprises a catalytically effective amount of cobalt.
10. A process for the catalytic hydrotreating of a hydrocarbon-containing feedstock in the presence of a hydrotreating catalyst according to any one of the preceding claims.
11. A process according to claim 10, wherein the hydrocarbon feedstock is characterised by having at least 50% of its components boiling above 524"C.
12. A process according to claim 10 or 11, wherein the hydrotreating is performed at a temperature of from 3710Cto 483"C.
13. A process according to any one of claims 10 - 12, wherein the hydrotreating is operated at a conversion of at least 50%, based on components boiling above 524"C.
14. A catalyst substantially as disclosed herein with reference to the Example.
15. A process for catalytic hydrotreating of a hydrocarbon-containing feedstock in the presence of a hydrotreating catalyst according to claim 14.
16. Any novel feature or combination of feature disclosed herein.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US20894880A | 1980-11-21 | 1980-11-21 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| GB2087747A true GB2087747A (en) | 1982-06-03 |
| GB2087747B GB2087747B (en) | 1984-07-04 |
Family
ID=22776714
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB8135076A Expired GB2087747B (en) | 1980-11-21 | 1981-11-20 | Improvements in or relating to a hydrotreating catalyst |
Country Status (12)
| Country | Link |
|---|---|
| JP (1) | JPS5946666B2 (en) |
| AU (1) | AU540245B2 (en) |
| CA (1) | CA1159039A (en) |
| DE (1) | DE3145718A1 (en) |
| ES (1) | ES507340A1 (en) |
| FR (1) | FR2494597A1 (en) |
| GB (1) | GB2087747B (en) |
| IT (1) | IT1143446B (en) |
| MX (2) | MX172430B (en) |
| NL (1) | NL8105267A (en) |
| SE (1) | SE448951B (en) |
| ZA (1) | ZA817732B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012213A1 (en) * | 1998-09-01 | 2000-03-09 | Japan Energy Corporation | Hydrocracking catalyst, producing method thereof, and hydrocracking method |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3522538A1 (en) * | 1984-06-22 | 1986-01-02 | Chiyoda Chemical Engineering & Construction Co. Ltd., Yokohama, Kanagawa | Process and catalyst for the hydrogenation of coal tar pitch |
| EP0178774B1 (en) * | 1984-09-12 | 1991-02-20 | Nippon Kokan Kabushiki Kaisha | A hydrogenation catalyst for coal tar, a method of hydrogenation of coal tar with use of such catalyst, and a method of producing super needle coke from the hydrogenation product of coal tar |
| JP4493997B2 (en) * | 2003-12-10 | 2010-06-30 | 財団法人石油産業活性化センター | Hydrodesulfurization catalyst for hydrocarbon oil and method for producing the same |
| US8110527B2 (en) | 2006-08-11 | 2012-02-07 | China Petroleum & Chemical Corporation | Alumina having a complex pore structure, and catalyst and process for selective hydrogenation of cracking gasoline |
| JP4902424B2 (en) * | 2007-05-21 | 2012-03-21 | Ｊｘ日鉱日石エネルギー株式会社 | Hydrorefining catalyst and hydrorefining method |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL261905A (en) * | 1960-03-02 | |||
| US3361526A (en) * | 1964-06-19 | 1968-01-02 | Grace W R & Co | Process for producing alumina having a narrow pore size distribution |
| CA943944A (en) * | 1967-10-27 | 1974-03-19 | Michael C. Chervenak | Catalysts, methods of preparation of same and processes for using same |
| JPS5141641B2 (en) * | 1972-01-06 | 1976-11-11 | ||
| US3952069A (en) * | 1973-01-26 | 1976-04-20 | Gulf Research & Development Company | Hydrogenation of aromatics |
| JPS51122105A (en) * | 1975-04-18 | 1976-10-26 | Toa Nenryo Kogyo Kk | Process for hydrofining of hydrocarbon oil |
| US4013547A (en) * | 1976-01-22 | 1977-03-22 | Union Oil Company Of California | Desulfurization of residual petroleum oils with a catalyst calcined at higher temperatures |
| US4301037A (en) * | 1980-04-01 | 1981-11-17 | W. R. Grace & Co. | Extruded alumina catalyst support having controlled distribution of pore sizes |
-
1981
- 1981-11-05 CA CA000389545A patent/CA1159039A/en not_active Expired
- 1981-11-09 ZA ZA817732A patent/ZA817732B/en unknown
- 1981-11-13 AU AU77476/81A patent/AU540245B2/en not_active Ceased
- 1981-11-19 DE DE19813145718 patent/DE3145718A1/en active Granted
- 1981-11-19 FR FR8121684A patent/FR2494597A1/en active Granted
- 1981-11-19 MX MX016070A patent/MX172430B/en unknown
- 1981-11-19 MX MX190208A patent/MX160789A/en unknown
- 1981-11-20 SE SE8106925A patent/SE448951B/en not_active IP Right Cessation
- 1981-11-20 JP JP56187655A patent/JPS5946666B2/en not_active Expired
- 1981-11-20 NL NL8105267A patent/NL8105267A/en not_active Application Discontinuation
- 1981-11-20 ES ES507340A patent/ES507340A1/en not_active Expired
- 1981-11-20 GB GB8135076A patent/GB2087747B/en not_active Expired
- 1981-11-20 IT IT49747/81A patent/IT1143446B/en active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2000012213A1 (en) * | 1998-09-01 | 2000-03-09 | Japan Energy Corporation | Hydrocracking catalyst, producing method thereof, and hydrocracking method |
| US6551500B1 (en) | 1998-09-01 | 2003-04-22 | Japan Energy Corporation | Hydrocracking catalyst, producing method thereof, and hydrocracking method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5946666B2 (en) | 1984-11-14 |
| GB2087747B (en) | 1984-07-04 |
| AU7747681A (en) | 1982-05-27 |
| MX160789A (en) | 1990-05-17 |
| SE448951B (en) | 1987-03-30 |
| ES507340A0 (en) | 1985-03-01 |
| IT1143446B (en) | 1986-10-22 |
| FR2494597B1 (en) | 1985-01-04 |
| IT8149747A0 (en) | 1981-11-20 |
| AU540245B2 (en) | 1984-11-08 |
| CA1159039A (en) | 1983-12-20 |
| NL8105267A (en) | 1982-06-16 |
| ZA817732B (en) | 1982-10-27 |
| SE8106925L (en) | 1982-05-22 |
| ES507340A1 (en) | 1985-03-01 |
| DE3145718A1 (en) | 1982-06-16 |
| MX172430B (en) | 1993-12-16 |
| DE3145718C2 (en) | 1987-06-19 |
| FR2494597A1 (en) | 1982-05-28 |
| JPS57117343A (en) | 1982-07-21 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0876443B1 (en) | Hydroconversion process employing a catalyst with specified pore size distribution and no added silica | |
| US5221656A (en) | Hydroprocessing catalyst | |
| US4686030A (en) | Mild hydrocracking with a catalyst having a narrow pore size distribution | |
| CA1170246A (en) | Residua demetalation/desulfurization catalyst and methods for its use | |
| US4255253A (en) | Hydrogen processing of hydrocarbon feeds using coated catalysts | |
| CA1117456A (en) | Process for the cracking of heavy hydrocarbon streams | |
| US4181602A (en) | Process for the hydrotreating of heavy hydrocarbon streams | |
| US4431525A (en) | Three-catalyst process for the hydrotreating of heavy hydrocarbon streams | |
| CA2093410C (en) | Improved hydroconversion process employing catalyst with specified pore size distribution | |
| US4434048A (en) | Hydrotreating catalyst and use thereof | |
| US4404097A (en) | Residua demetalation/desulfurization catalyst and methods for its use | |
| US4657664A (en) | Process for demetallation and desulfurization of heavy hydrocarbons | |
| CA1129839A (en) | Hydrotreating a hydrocarbon stream to remove nitrogen and sulfur | |
| US4188284A (en) | Process for the hydrotreating of heavy hydrocarbon streams | |
| US4414141A (en) | Hydrotreating catalyst | |
| EP0686687A1 (en) | Mild hydrocracking of heavy hydrocarbon feedstocks employing silica-alumina catalysts | |
| CA1273311A (en) | Process for demetallation and desulfurization of heavy hydrocarbons | |
| US4493761A (en) | Catalytic hydroliquefaction using a Cr-Mo-Group VIII catalyst | |
| CA1187468A (en) | Hydrotreating catalyst and process | |
| EP0070125B1 (en) | Crystalline silica zeolite-containing catalyst and hydrocarbon hydroprocess utilizing the catalyst | |
| CA2190392A1 (en) | Stacked bed catalyst system for deep hydrosulfurization | |
| US5322829A (en) | Resid hydrotreating catalyst and process | |
| CA1102729A (en) | Process for the hydrotreating of heavy hydrocarbon streams | |
| GB2087747A (en) | Improvements in or relating to a hydrotreating catalyst | |
| JP3378402B2 (en) | Desulfurization method of catalytic cracking gasoline |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PCNP | Patent ceased through non-payment of renewal fee |
Effective date: 19961120 |