CA1228561A - Process for converting olefins to distillate and/or lube oil products - Google Patents
Process for converting olefins to distillate and/or lube oil productsInfo
- Publication number
- CA1228561A CA1228561A CA000433564A CA433564A CA1228561A CA 1228561 A CA1228561 A CA 1228561A CA 000433564 A CA000433564 A CA 000433564A CA 433564 A CA433564 A CA 433564A CA 1228561 A CA1228561 A CA 1228561A
- Authority
- CA
- Canada
- Prior art keywords
- olefin
- distillate
- aromatic hydrocarbon
- lube oil
- oil products
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/20—Organic compounds not containing metal atoms
- C10G29/205—Organic compounds not containing metal atoms by reaction with hydrocarbons added to the hydrocarbon oil
-
- 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
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
-
- 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
- C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
- C10G50/02—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation of hydrocarbon oils for lubricating purposes
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A PROCESS FOR CONVERTING OLEFINS TO
DISTILLATE AND/OR LUBE OIL PRODUCTS
Abstract A process for converting olefins to distillate and/or lube oil products comprises contacting under conversion conditions an olefin with a crystalline aluminosilicate zeolite having a silica to alumina mole ratio of at least 12 and a constraint index within the range of 1 to 12 in the presence of a reactive aromatic hydrocarbon; said olefin and said reactive aromatic hydrocarbon being present in a molar ratio of 10:1 to 1:1.
DISTILLATE AND/OR LUBE OIL PRODUCTS
Abstract A process for converting olefins to distillate and/or lube oil products comprises contacting under conversion conditions an olefin with a crystalline aluminosilicate zeolite having a silica to alumina mole ratio of at least 12 and a constraint index within the range of 1 to 12 in the presence of a reactive aromatic hydrocarbon; said olefin and said reactive aromatic hydrocarbon being present in a molar ratio of 10:1 to 1:1.
Description
85~
A PROCESS FOR CONVERTING OLEFINS TO
DISTILLATE AND/OR Lute OIL PRODUCTS
This invention relates to a process for converting olefins to distillate and/or lube oil products.
US. Patent No. 4,150,062 describes a process for the conversion of olefins having 2 to 4 carbon atoms to a product comprising a high octane gasoline component by contacting an appropriate olefin feed stock with a catalyst comprising a crystalline aluminosilicate zealot in the presence ox a relatively large amount of I water.
US. Patent No. 4,211,640 describes a catalytic process for the treatment of highly olefinic gasoline with an acidic crystalline aluminosilicate zealot to enhance the gum stability of said gasoline and produce products comprising w to gasoline and fuel oil.
The present invention it predicated on the discovery that when low molecular weight aromatic compounds are added to an olefin-to--gasoline distillate (Ovid) reaction product stream, the olefinic components in the stream will alkylate the aromatics to form both lube and diesel range materials. Lute oil produced thereby is in ir~reased yield and viscosity index.
Accordingly the present invention resides in a process for converting olefins to distillate and/or lube oil products, comprising contacting under conversion conditions an olefin With a crystalline aluminosilicate zealot having a silica to alumina mole retie of at least 12 and a constraint index within the range of 1 to 12 in a reaction zone in the presence of a reactive aromatic hydrocarbon; set Olin and said reactive aromatic hydrocarbon being present in the molar ratio of lû:l to 1:1.
The olefins used in the present process may be any of those I employed in conventional OLD technology and include moo- and dolphins of 2 to 10 carbon atoms, such as ethene and propane;
cycloole~ins of to 10 car w n atoms, such as cyclobutene and cyclopentene; and olefins alkylated to aromatic rings with less than 10 Jo Sue carbon atoms. Preferred olefins have 2 to 7 croon atoms. In addition, reactive olefinic products of OLD reactions can be used as the feed stream in the present process. In other words, the aromatic compounds may be added directly to the reaction zone with the unrequited olefin or it may be added to the reaction zone after the olefin-to-gasoline distillate reaction has had an opportunity-to provide some long-chain oiliness. In any event, a product of increased lube yield and, higher viscosity index will be provided. because of the high value of lube oil relative to lighter distillate, there is incentive to I maximize lube product.
The aromatic hydrocarbons used in the present process may contain one or two aromatic rings, including aromatic rings alkylated with one or more saturated or unsaturated groups, and including aromatic rings connected to saturated rings such as tetralin, methyltetralin and ethyltetralin. In addition to a pure aromatic feed, it is possible to employ a refinery stream rich in aromatics such as a reformat cut. It a stream rich in both olefins and aromatics, such as an FCC gasoline, is used the oleFins will also take part in the olefin-to-gasoline~distillate reaction.
The catalyst used in the present process is a crystalline aluminosilicate zealot havincJ a silica to alumina mole ratio Clue at least 12 and a constraint index of 1 to 12. Examples of such a zealot are ZSM-5, ZSM-ll, ZSM-12, Z5~-35 and ZS~-38. Zealot ZSM-5 is described in US. Patent No. 3,702,886; ZSM-ll is described In US.
Patent No. 3,709,979; ZSM-12 is described in US. Patent No. 3,B38,44g;
ZSM-35 is described in US. Patent No. 4,016,245; and ZS~-38 is described in US. Patent No. 4,046,859.
It should also be noted that natural zealots may sometimes be converted to this type zealot catalyst by various activation I procedures and other treatments such as base exchange, steaming, alumina extraction and calcination or some combination thereon.
Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heulandite and clinoptilolite.
~L~2~5~j~
The preferred crystal aluminosilicate zealots are ZSM-5 and ZSM-12.
Conveniently, the zealot catalyst is employed in combination with a support or a binder, such as for example, a porous inorganic S oxide support or a clay binder. Examples of such binder materials include alumina, zircon, silica, magnesia, Thor, titanic, bone and combinations thereof, generally in the form of dried inorganic oxide gels and gelatinous precipitates. Suitable clay materials include, by way of example, bentonite and kieselguhr. The amount of alumina-I silicate zealot to the total composition of catalyst and binder or support may vary between owe to go by weight, and more usually in the range of owe to owe by weight of the composition.
The operating conditions employed in the present process, particularly the temperature, pressure, space velocity, molar ratio a aromatic to olefin reactants, absence of added hydrogen, and the preserve of any delineates are chosen so to promote reaction between the aromatics and the OG/0 product distillate to produce long-chain all aromatics and thereby increase lube oil yield and viscosity index.
Suitable operating conditions include a temperature from 204 to 427C
(400 to 800F), a pressure from 791 to 17339 spa (100 to 2500 prig), and a LhSV from 0.2 to 20 per hour. Preferred conditions include a temperature from 2~2 to 316C (450 to 600F~, a pressure from 4238 to 6990 spa (600 to 1000 prig), and a L~SV from 0.5 to 2 and most preferably from 1 to 1.5. The molar ratio of olefins to reactive aromatic hydrocarbon may vary from 10:1 to 1:1. Preferred, as reactive hydrocarbons, are aromatic hydrocar w no and alkyl-substituted cyclic hydrocarbons, or alkyd aromatic cyclic hydrocarbons. Also, it desired, any suitable delineate known in the art may be used.
The advantageous results obtainable with the process of tune I present invention are illustrated by Tale 1 which shows the effect on viscosity index of' Audrey alkyd chains to Roth Cyril and dicyclic aromatics. As Jill be seen prom the Tale, the highest viscosity indices are achieved by adding loft straight allele chains, but some viscosity index improvement it ODtaine~ with highly substituted compounds.
F-1865 I 122~35~
Viscosity Index of Some High MOW. Alkyd Aromatics l-Alpha-Naphthyl-Undecane C21H30 111 VI
l-Alpha-Naphthyl-Pentadecane C25 8 119 VI
9-p-Tolyoctadecane C C25H44 109 VI
l-Phenyleicosane C20 ~26H46 160 VI
A PROCESS FOR CONVERTING OLEFINS TO
DISTILLATE AND/OR Lute OIL PRODUCTS
This invention relates to a process for converting olefins to distillate and/or lube oil products.
US. Patent No. 4,150,062 describes a process for the conversion of olefins having 2 to 4 carbon atoms to a product comprising a high octane gasoline component by contacting an appropriate olefin feed stock with a catalyst comprising a crystalline aluminosilicate zealot in the presence ox a relatively large amount of I water.
US. Patent No. 4,211,640 describes a catalytic process for the treatment of highly olefinic gasoline with an acidic crystalline aluminosilicate zealot to enhance the gum stability of said gasoline and produce products comprising w to gasoline and fuel oil.
The present invention it predicated on the discovery that when low molecular weight aromatic compounds are added to an olefin-to--gasoline distillate (Ovid) reaction product stream, the olefinic components in the stream will alkylate the aromatics to form both lube and diesel range materials. Lute oil produced thereby is in ir~reased yield and viscosity index.
Accordingly the present invention resides in a process for converting olefins to distillate and/or lube oil products, comprising contacting under conversion conditions an olefin With a crystalline aluminosilicate zealot having a silica to alumina mole retie of at least 12 and a constraint index within the range of 1 to 12 in a reaction zone in the presence of a reactive aromatic hydrocarbon; set Olin and said reactive aromatic hydrocarbon being present in the molar ratio of lû:l to 1:1.
The olefins used in the present process may be any of those I employed in conventional OLD technology and include moo- and dolphins of 2 to 10 carbon atoms, such as ethene and propane;
cycloole~ins of to 10 car w n atoms, such as cyclobutene and cyclopentene; and olefins alkylated to aromatic rings with less than 10 Jo Sue carbon atoms. Preferred olefins have 2 to 7 croon atoms. In addition, reactive olefinic products of OLD reactions can be used as the feed stream in the present process. In other words, the aromatic compounds may be added directly to the reaction zone with the unrequited olefin or it may be added to the reaction zone after the olefin-to-gasoline distillate reaction has had an opportunity-to provide some long-chain oiliness. In any event, a product of increased lube yield and, higher viscosity index will be provided. because of the high value of lube oil relative to lighter distillate, there is incentive to I maximize lube product.
The aromatic hydrocarbons used in the present process may contain one or two aromatic rings, including aromatic rings alkylated with one or more saturated or unsaturated groups, and including aromatic rings connected to saturated rings such as tetralin, methyltetralin and ethyltetralin. In addition to a pure aromatic feed, it is possible to employ a refinery stream rich in aromatics such as a reformat cut. It a stream rich in both olefins and aromatics, such as an FCC gasoline, is used the oleFins will also take part in the olefin-to-gasoline~distillate reaction.
The catalyst used in the present process is a crystalline aluminosilicate zealot havincJ a silica to alumina mole ratio Clue at least 12 and a constraint index of 1 to 12. Examples of such a zealot are ZSM-5, ZSM-ll, ZSM-12, Z5~-35 and ZS~-38. Zealot ZSM-5 is described in US. Patent No. 3,702,886; ZSM-ll is described In US.
Patent No. 3,709,979; ZSM-12 is described in US. Patent No. 3,B38,44g;
ZSM-35 is described in US. Patent No. 4,016,245; and ZS~-38 is described in US. Patent No. 4,046,859.
It should also be noted that natural zealots may sometimes be converted to this type zealot catalyst by various activation I procedures and other treatments such as base exchange, steaming, alumina extraction and calcination or some combination thereon.
Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heulandite and clinoptilolite.
~L~2~5~j~
The preferred crystal aluminosilicate zealots are ZSM-5 and ZSM-12.
Conveniently, the zealot catalyst is employed in combination with a support or a binder, such as for example, a porous inorganic S oxide support or a clay binder. Examples of such binder materials include alumina, zircon, silica, magnesia, Thor, titanic, bone and combinations thereof, generally in the form of dried inorganic oxide gels and gelatinous precipitates. Suitable clay materials include, by way of example, bentonite and kieselguhr. The amount of alumina-I silicate zealot to the total composition of catalyst and binder or support may vary between owe to go by weight, and more usually in the range of owe to owe by weight of the composition.
The operating conditions employed in the present process, particularly the temperature, pressure, space velocity, molar ratio a aromatic to olefin reactants, absence of added hydrogen, and the preserve of any delineates are chosen so to promote reaction between the aromatics and the OG/0 product distillate to produce long-chain all aromatics and thereby increase lube oil yield and viscosity index.
Suitable operating conditions include a temperature from 204 to 427C
(400 to 800F), a pressure from 791 to 17339 spa (100 to 2500 prig), and a LhSV from 0.2 to 20 per hour. Preferred conditions include a temperature from 2~2 to 316C (450 to 600F~, a pressure from 4238 to 6990 spa (600 to 1000 prig), and a L~SV from 0.5 to 2 and most preferably from 1 to 1.5. The molar ratio of olefins to reactive aromatic hydrocarbon may vary from 10:1 to 1:1. Preferred, as reactive hydrocarbons, are aromatic hydrocar w no and alkyl-substituted cyclic hydrocarbons, or alkyd aromatic cyclic hydrocarbons. Also, it desired, any suitable delineate known in the art may be used.
The advantageous results obtainable with the process of tune I present invention are illustrated by Tale 1 which shows the effect on viscosity index of' Audrey alkyd chains to Roth Cyril and dicyclic aromatics. As Jill be seen prom the Tale, the highest viscosity indices are achieved by adding loft straight allele chains, but some viscosity index improvement it ODtaine~ with highly substituted compounds.
F-1865 I 122~35~
Viscosity Index of Some High MOW. Alkyd Aromatics l-Alpha-Naphthyl-Undecane C21H30 111 VI
l-Alpha-Naphthyl-Pentadecane C25 8 119 VI
9-p-Tolyoctadecane C C25H44 109 VI
l-Phenyleicosane C20 ~26H46 160 VI
2-phenyleicosane c~c18 C26H46 15C VI
1,4-Di-n-Decylbenzene C10 C26H4~ 154 VI
C1c 2,4,6-Trimethyl-n-octa- C27H~8 121 VI
decylbenzene C
2(Ar)Decyltetralin C10 C20H32 140 VI
C6 c 7(Ar)n-Butyl-l-n-Hexyl- 4 C20 2 94 VI
tetralin EXAMPLE
An OG~3 distillate having the Following properties was produced by reaction of a C3 C4 Olin over an ~ZSM-12 extradite catalyst containing 65æ of the zealot with a Sue molar ratio of 123:1 and 35~ of an alumina binder at awoke (450F) and 4238 spa (owe ,osig).
Bromide No. BYWAY
Aniline No. 155 Distillation: I OF (C) 356 lo 37~ lug owe 422 ~217) act 496 (258~
95~ 604 (31B) 99.5~ ~06 (31~) ~85~i~
Table 2 compares the results obtained by contacting the resultant distillate with the same ZSM-12 catalyst at a LHSV of 1.0 an a pressure of 1000 prig (6996 spa) with and without the addition of an aromatic compound in the form of Bunsen.
Reaction ox OLD Distillate Over ZSM I
OLD Distillate 8C~ ùG/D Dist./2C~6 ensign Days on Stream 1.5 2.5 3.5 4.5 5.5 6.6 7.5 Of 450 500 550 450 500 550 6~0 (C) (232)(260) (288)(232) (260) (288)(316) Product APE
æ 650F (343C) inn 10.4 9.9 7.1 7.0 7.3 9.8 350f (177C) cut --- All duct Composite & Distilled ---380F~ (193C) Product Composite APE 46.7 47.1 Aniline No. 167 162 % 670F (354C)+ 9.0 7.0 APE 37.5 ~7.6 TV ~340C 21.94 21~7~
TV Q100C 4.352 4.395 SUP luff (38C) 114.7 113.8 SUP @130F ~54C) 70.8 70.7 SUP ~210F (99C) 40.9 41.0 viscosity Index 105.6 111.1
1,4-Di-n-Decylbenzene C10 C26H4~ 154 VI
C1c 2,4,6-Trimethyl-n-octa- C27H~8 121 VI
decylbenzene C
2(Ar)Decyltetralin C10 C20H32 140 VI
C6 c 7(Ar)n-Butyl-l-n-Hexyl- 4 C20 2 94 VI
tetralin EXAMPLE
An OG~3 distillate having the Following properties was produced by reaction of a C3 C4 Olin over an ~ZSM-12 extradite catalyst containing 65æ of the zealot with a Sue molar ratio of 123:1 and 35~ of an alumina binder at awoke (450F) and 4238 spa (owe ,osig).
Bromide No. BYWAY
Aniline No. 155 Distillation: I OF (C) 356 lo 37~ lug owe 422 ~217) act 496 (258~
95~ 604 (31B) 99.5~ ~06 (31~) ~85~i~
Table 2 compares the results obtained by contacting the resultant distillate with the same ZSM-12 catalyst at a LHSV of 1.0 an a pressure of 1000 prig (6996 spa) with and without the addition of an aromatic compound in the form of Bunsen.
Reaction ox OLD Distillate Over ZSM I
OLD Distillate 8C~ ùG/D Dist./2C~6 ensign Days on Stream 1.5 2.5 3.5 4.5 5.5 6.6 7.5 Of 450 500 550 450 500 550 6~0 (C) (232)(260) (288)(232) (260) (288)(316) Product APE
æ 650F (343C) inn 10.4 9.9 7.1 7.0 7.3 9.8 350f (177C) cut --- All duct Composite & Distilled ---380F~ (193C) Product Composite APE 46.7 47.1 Aniline No. 167 162 % 670F (354C)+ 9.0 7.0 APE 37.5 ~7.6 TV ~340C 21.94 21~7~
TV Q100C 4.352 4.395 SUP luff (38C) 114.7 113.8 SUP @130F ~54C) 70.8 70.7 SUP ~210F (99C) 40.9 41.0 viscosity Index 105.6 111.1
Claims (8)
1. A process for converting olefins to distillate and/or lube oil products, comprising contacting under conversion conditions an olefin with a crystalline aluminosilicate zeolite having a silica to alumina mole ratio of at least 12 and a constraint index within the range of 1 to 12 in a reaction zone in the presence of a reactive aromatic hydrocarbon; said olefin and said reactive aromatic hydrocarbon being present in the molar ratio of 10:1 to 1:1.
2. A process as claimed in claim 1, wherein the olefin has 2 to 10 carbon atoms.
3. A process as claimed in claim 1, wherein the olefin has 2 to 7 carbon atoms.
4. A process as claimed in claim 1, 2 or 3 wherein the reactive aromatic hydrocarbon is introduced into the reaction zone after the olefin has been converted by contact with the zeolite into a stream containing long chain olefinic compounds.
5. A process as claimed in claim 1, 2 or 3 wherein the reactive aromatic hydrocarbon and unreacted olefin are introduced simultaneously into the reaction zone.
6. A process as claimed in claim 1, 2 or 3 wherein the conversion conditions include a temperature of 204 to 427°C (400 to 800°F), a pressure of 791 to 17339 kPa (100 to 2500 psig) and a LHSV
from 0.2 to 20 per hour.
from 0.2 to 20 per hour.
7. A process as claimed in claim 1, 2 or 3 wherein the conversion conditions include a temperature of 232 to 316°C (450 to 650°F), a pressure of 4238 to 6990 kPa (600 to 1000 psig) and a LHSV of 0.5 to 2.
8. A process as claimed in claim 1, 2 or 3 wherein the zeolite is ZSM-5 or ZSM-12.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US42602782A | 1982-09-28 | 1982-09-28 | |
| US426,027 | 1982-09-28 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1228561A true CA1228561A (en) | 1987-10-27 |
Family
ID=23688982
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000433564A Expired CA1228561A (en) | 1982-09-28 | 1983-07-29 | Process for converting olefins to distillate and/or lube oil products |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0104729A3 (en) |
| JP (1) | JPS5980490A (en) |
| AU (1) | AU1748883A (en) |
| CA (1) | CA1228561A (en) |
| ZA (1) | ZA835854B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5132477A (en) * | 1991-04-29 | 1992-07-21 | Mobil Oil Corporation | Process for producing alkylaromatic lubricant fluids |
| US9637423B1 (en) | 2014-12-16 | 2017-05-02 | Exxonmobil Research And Engineering Company | Integrated process for making high-octane gasoline |
| US9637424B1 (en) | 2014-12-16 | 2017-05-02 | Exxonmobil Research And Engineering Company | High octane gasoline and process for making same |
| US10023533B2 (en) | 2014-12-16 | 2018-07-17 | Exxonmobil Research And Engineering Company | Process to produce paraffinic hydrocarbon fluids from light paraffins |
| US9688626B2 (en) | 2014-12-16 | 2017-06-27 | Exxonmobil Research And Engineering Company | Upgrading paraffins to distillates and lubricant basestocks |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE755959A (en) * | 1969-09-12 | 1971-02-15 | Snam Progetti | SYNTHETIC LUBRICATING OILS WITH VERY VISCOSITY |
| GB1525423A (en) * | 1976-05-12 | 1978-09-20 | Mobil Oil Corp | Alkylation/transalkylation in presence of crystalline aluminosilicate catalyst |
| CA1135286A (en) * | 1978-12-14 | 1982-11-09 | Mobil Oil Corporation | Alkylation of aromatic hydrocarbons |
-
1983
- 1983-07-29 CA CA000433564A patent/CA1228561A/en not_active Expired
- 1983-08-01 AU AU17488/83A patent/AU1748883A/en not_active Abandoned
- 1983-08-02 EP EP83304451A patent/EP0104729A3/en not_active Withdrawn
- 1983-08-09 ZA ZA835854A patent/ZA835854B/en unknown
- 1983-09-28 JP JP58178356A patent/JPS5980490A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| EP0104729A3 (en) | 1986-08-27 |
| EP0104729A2 (en) | 1984-04-04 |
| AU1748883A (en) | 1984-04-05 |
| ZA835854B (en) | 1985-03-27 |
| JPS5980490A (en) | 1984-05-09 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |