CA1205824A - Process for producing tert.butyl alkyl ethers in the presence of butadiene - Google Patents
Process for producing tert.butyl alkyl ethers in the presence of butadieneInfo
- Publication number
- CA1205824A CA1205824A CA000421707A CA421707A CA1205824A CA 1205824 A CA1205824 A CA 1205824A CA 000421707 A CA000421707 A CA 000421707A CA 421707 A CA421707 A CA 421707A CA 1205824 A CA1205824 A CA 1205824A
- Authority
- CA
- Canada
- Prior art keywords
- reactors
- butadiene
- reactor
- alkyl ethers
- reactants
- 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
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/01—Preparation of ethers
- C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
- C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C43/00—Ethers; Compounds having groups, groups or groups
- C07C43/02—Ethers
- C07C43/03—Ethers having all ether-oxygen atoms bound to acyclic carbon atoms
- C07C43/04—Saturated ethers
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C43/00—Ethers; Compounds having groups, groups or groups
- C07C43/02—Ethers
- C07C43/03—Ethers having all ether-oxygen atoms bound to acyclic carbon atoms
- C07C43/04—Saturated ethers
- C07C43/06—Diethyl ether
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
"PROCESS FOR PRODUCING TERT.BUTYL ALKYL ETHERS IN THE PRESENCE
OF BUTADIENE"
ABSTRACT
In producing tert.butyl alkyl ethers starting from a hydrocarbon feedstock containing butadiene in addition to isobutene, the increase in the pressure drops through the etherification reactors due to the butadiene is eliminated by feeding the reactants from the bottom upwards.
OF BUTADIENE"
ABSTRACT
In producing tert.butyl alkyl ethers starting from a hydrocarbon feedstock containing butadiene in addition to isobutene, the increase in the pressure drops through the etherification reactors due to the butadiene is eliminated by feeding the reactants from the bottom upwards.
Description
```` ~2~
- 1 - CASE 1ll73 DESCRIPTION
This invention relates to a process for producins tert~butyl alkyl ethers in the presenee of butadiene.
The reaction of addition oE alcohols to tertiary olefins æuch as isobutene to produce tert.butyl alkyl ethers is an exothermic reaction t~ich is acid-catalysed~
In the presence of suitable catalysts such as macroporous ion exchange resins, the reaction proceeds to equilibrium in times which are of industrial interest, even at relati~ely low temper_ atures t40-50c).
It is kno~m that it is not neeessary to operate with high purity isobutene, and instead any cut which contains it is suitable, as the alcohol addition takes place selectively to the double bonds which engage a tertiary carbon atom. Those cuts originating from eatalytic cracking and those originating from steam cracking, these latter either before or after eYtracting the buiadiene~ are particularly suitable.
When usin~ as olefin feedstock the C4 fraetion from catalytic eracking or that fro~ steam cracking after extractirlg the butadiene~
and using methanol or ethanol as the alcohol an~ a sulpnonie maeroporous resin type Amberlyst l5 or Lewatit SPC 108 as the eatalystl tne reaetion can be used industrially within a wide range of reactor designs and operating conditions direeted towards optimisir.g the conversio~ of one or other o~ the reactants~ I~
these cases, high selectivity is alwa~s obtained, together wtith good perf~rmance of the catalyst both in terms of catalytie aetivity a~d life.
':t,~
"
- 1 - CASE 1ll73 DESCRIPTION
This invention relates to a process for producins tert~butyl alkyl ethers in the presenee of butadiene.
The reaction of addition oE alcohols to tertiary olefins æuch as isobutene to produce tert.butyl alkyl ethers is an exothermic reaction t~ich is acid-catalysed~
In the presence of suitable catalysts such as macroporous ion exchange resins, the reaction proceeds to equilibrium in times which are of industrial interest, even at relati~ely low temper_ atures t40-50c).
It is kno~m that it is not neeessary to operate with high purity isobutene, and instead any cut which contains it is suitable, as the alcohol addition takes place selectively to the double bonds which engage a tertiary carbon atom. Those cuts originating from eatalytic cracking and those originating from steam cracking, these latter either before or after eYtracting the buiadiene~ are particularly suitable.
When usin~ as olefin feedstock the C4 fraetion from catalytic eracking or that fro~ steam cracking after extractirlg the butadiene~
and using methanol or ethanol as the alcohol an~ a sulpnonie maeroporous resin type Amberlyst l5 or Lewatit SPC 108 as the eatalystl tne reaetion can be used industrially within a wide range of reactor designs and operating conditions direeted towards optimisir.g the conversio~ of one or other o~ the reactants~ I~
these cases, high selectivity is alwa~s obtained, together wtith good perf~rmance of the catalyst both in terms of catalytie aetivity a~d life.
':t,~
"
2-~ihen o~eratin~ with an olefin cut with a high butadiene content~ such as the C4 cut from steam crackin~ before extractin~
the butadiene~ the operating conditions must be accurately defined in order to allow a butadiene recovery exceeding ~8 ~. In particular7 it is necessary to maintain a strict relationship between the temperature and spacial velocity as described in USA
Patent 4,039,590.
- It has howsver been noted that when carrying out the isobutene etheri~ication reaction in the presence of butadiene in a tu~ular reactor containinO a macroporous resin7 and feeding the reactants from the top downwards in the nor~nal manner, an increase in pressure drops takes place with time~ even 1.rhen operating ~lnder conditions which allow a high butadiene recovery of ~ 99%, and in addition a slight conversion fall-off~
t 15 However, an identical test carried out with a butadiene~free cut shows neither pressure drop increases nor conversion reductions.
It has been surprisingly found, and constitutes the subject matter of the present invention9 that by feeding the butadiene containing ~ feedstocks so that they flow from the bottom upward6~ under slight `~ - 20 bed expansion conditions, the pressure drops remain constant with timeO
The process according to the present invention consists of producing tert.butyl alkyl ethers by reacting the isobutylene o~ a hydro-carbon feedstock which also contains butadiene at concentrations of between 10 clnd 70% by weiOnt~ with one or more aliphatic alcohols~ preferably methanol or ethanol~ in one~ two or more reactors~ preferably in series, and is characterised in that the ., ' . .
~058Z9L
.~ _ 3 reactants (hydrocarbon feedstock containing butadiene and alcohol or alcohols) and the reaction products flow through the reactor or reactors from the bottom upwards.
The reactors may be provided with a macroporous acid ion exchange resin catalyst.
In addition to the ascendl~g direction of flow of the reactants and reaction products, the linear velocity of the reactants through the reactor or reactors may vary from 0.5 to 2 cm/sec. and the temperature in the reactors may range from 50 to 60C, preferably from 50 to 55C. Some examples are described hereinafter for the purpose of better illustrating the invention, but these must in no way be con-sidered as limitative thereof.
A C4 cut having the following composition:
Propylene0.46 % by weight Isobutane6.87 % by weight n-butane11.80 ~.by weight Butene-l11.39 % by weight Isobutene30.19 % by weight Butene-2+3.25 % by weight Cis butene-21.55 % by weight Butadiene34.43 % by weight in mixed with methanol such that the molar isvbutene/methanol ratio is equal to 0.85, and the mixture is fed at a through-put of 14 l/h and a temperature of 50C through two reactors connected ln series, having a total capacity of 4~5 litres and filled with 4 litres of catalyst. The catalyst is a macroporous sulphonic resin with an .," .,~,j, 5~Z~
~, exchange capacity of 4~8 meq H+/g dry.
The reactants flow from the botto~ up~ards~
The linear veloclty is 1 cm/sec.
The conrersion and pressure drops with respect to time are as ~ollo~ls - Time hours 24 5002000 - ~ P 1st reactor kg/cm2 0.2 0.2 0.2 - ~ P 2nd reactor kg/cm 0.2 002 0.2 - % ~rEE by weight 38.1 38 38 - ,' dimers and codimers by weight 0.05 0.05 0.0 - % butenyl ethers by weight 0.2 0~150.2 - isobutene conversion 9606 96~496.4 - butadiene recovery ~ 99 ~ 9g ~ 99 - ~ P represents pressure drop.
15 EXA~LE 2 (comparative) The feedstock described in the preceding example is fed under the same temperature and spacial ~elocity conditions to the two reactor~ connected in series, but in such a manner that the flow direction of the reactants is from the top downwards.
At the beginning o~ the test, the results are analogous to those of the preceding example, but ~s time passes a progressiv~ pressure drop increase and a slight con~ersion fall-o~ are obser~ed.
_ Time hours 24 500 2000 - ~ P 1st reactor k ~cm2 o ~ ~.4 1.5 - ~ P 2nd reactor kg/c~2 0.3 005 1~8 _ 76 ~rBE by weight 38 37-9 36 _ % dimers and codimers by wei~ht 0~1 0,1 0.05 . ~
51~2~
_ ~ butenyl ethers by weisht 0.2 0~2 0.2 - isobutene conversion 96.4 96.1 91.3 butadiene recovery ~99 >99 ~ 99 :~ EXAMPLE 3 (comparative) ; 5 Methanol i.s added to an olefin cut containing 35% of isobutene and O.ZY of butadiene by weight, such that the molar isobutene~methanol ratio.is o.8s.
` Tha mixture is fed at a throughput of 14 l/h and a temperature of -- 50C to the two reactors connected in series, the flow dlrectio:
being from the top downwards. In the absence of butadiene~ no . pres.sure drop increase or conversion fal].-off with time are observed.
Time hours 24 500 2000 - . P 1st reactor kg/cm2 0.3 0.3 0.3 :; 15 - L~ P 2nd reactor kg/crn o,3 o.3 o,3 - % ~TBE by weight 43.1 42.9 43 - ~ dimers and codimers by weight 0.3 0.3 0.2 _ isobutene conversi.on 96.8 9606 9606 -.:
the butadiene~ the operating conditions must be accurately defined in order to allow a butadiene recovery exceeding ~8 ~. In particular7 it is necessary to maintain a strict relationship between the temperature and spacial velocity as described in USA
Patent 4,039,590.
- It has howsver been noted that when carrying out the isobutene etheri~ication reaction in the presence of butadiene in a tu~ular reactor containinO a macroporous resin7 and feeding the reactants from the top downwards in the nor~nal manner, an increase in pressure drops takes place with time~ even 1.rhen operating ~lnder conditions which allow a high butadiene recovery of ~ 99%, and in addition a slight conversion fall-off~
t 15 However, an identical test carried out with a butadiene~free cut shows neither pressure drop increases nor conversion reductions.
It has been surprisingly found, and constitutes the subject matter of the present invention9 that by feeding the butadiene containing ~ feedstocks so that they flow from the bottom upward6~ under slight `~ - 20 bed expansion conditions, the pressure drops remain constant with timeO
The process according to the present invention consists of producing tert.butyl alkyl ethers by reacting the isobutylene o~ a hydro-carbon feedstock which also contains butadiene at concentrations of between 10 clnd 70% by weiOnt~ with one or more aliphatic alcohols~ preferably methanol or ethanol~ in one~ two or more reactors~ preferably in series, and is characterised in that the ., ' . .
~058Z9L
.~ _ 3 reactants (hydrocarbon feedstock containing butadiene and alcohol or alcohols) and the reaction products flow through the reactor or reactors from the bottom upwards.
The reactors may be provided with a macroporous acid ion exchange resin catalyst.
In addition to the ascendl~g direction of flow of the reactants and reaction products, the linear velocity of the reactants through the reactor or reactors may vary from 0.5 to 2 cm/sec. and the temperature in the reactors may range from 50 to 60C, preferably from 50 to 55C. Some examples are described hereinafter for the purpose of better illustrating the invention, but these must in no way be con-sidered as limitative thereof.
A C4 cut having the following composition:
Propylene0.46 % by weight Isobutane6.87 % by weight n-butane11.80 ~.by weight Butene-l11.39 % by weight Isobutene30.19 % by weight Butene-2+3.25 % by weight Cis butene-21.55 % by weight Butadiene34.43 % by weight in mixed with methanol such that the molar isvbutene/methanol ratio is equal to 0.85, and the mixture is fed at a through-put of 14 l/h and a temperature of 50C through two reactors connected ln series, having a total capacity of 4~5 litres and filled with 4 litres of catalyst. The catalyst is a macroporous sulphonic resin with an .," .,~,j, 5~Z~
~, exchange capacity of 4~8 meq H+/g dry.
The reactants flow from the botto~ up~ards~
The linear veloclty is 1 cm/sec.
The conrersion and pressure drops with respect to time are as ~ollo~ls - Time hours 24 5002000 - ~ P 1st reactor kg/cm2 0.2 0.2 0.2 - ~ P 2nd reactor kg/cm 0.2 002 0.2 - % ~rEE by weight 38.1 38 38 - ,' dimers and codimers by weight 0.05 0.05 0.0 - % butenyl ethers by weight 0.2 0~150.2 - isobutene conversion 9606 96~496.4 - butadiene recovery ~ 99 ~ 9g ~ 99 - ~ P represents pressure drop.
15 EXA~LE 2 (comparative) The feedstock described in the preceding example is fed under the same temperature and spacial ~elocity conditions to the two reactor~ connected in series, but in such a manner that the flow direction of the reactants is from the top downwards.
At the beginning o~ the test, the results are analogous to those of the preceding example, but ~s time passes a progressiv~ pressure drop increase and a slight con~ersion fall-o~ are obser~ed.
_ Time hours 24 500 2000 - ~ P 1st reactor k ~cm2 o ~ ~.4 1.5 - ~ P 2nd reactor kg/c~2 0.3 005 1~8 _ 76 ~rBE by weight 38 37-9 36 _ % dimers and codimers by wei~ht 0~1 0,1 0.05 . ~
51~2~
_ ~ butenyl ethers by weisht 0.2 0~2 0.2 - isobutene conversion 96.4 96.1 91.3 butadiene recovery ~99 >99 ~ 99 :~ EXAMPLE 3 (comparative) ; 5 Methanol i.s added to an olefin cut containing 35% of isobutene and O.ZY of butadiene by weight, such that the molar isobutene~methanol ratio.is o.8s.
` Tha mixture is fed at a throughput of 14 l/h and a temperature of -- 50C to the two reactors connected in series, the flow dlrectio:
being from the top downwards. In the absence of butadiene~ no . pres.sure drop increase or conversion fal].-off with time are observed.
Time hours 24 500 2000 - . P 1st reactor kg/cm2 0.3 0.3 0.3 :; 15 - L~ P 2nd reactor kg/crn o,3 o.3 o,3 - % ~TBE by weight 43.1 42.9 43 - ~ dimers and codimers by weight 0.3 0.3 0.2 _ isobutene conversi.on 96.8 9606 9606 -.:
Claims (12)
1. A process for producing tert.butyl alkyl ethers by reacting the isobutylene of a hydrocarbon feedstock, which also contains butadiene at a concentration of between 10 and 70 % by weight, with one or more aliphatic alcohols in one, two or more reactors, characterised in that the reactants and the reaction products are made to flow the bottom upwards through the reactor or reactors.
2. A process as defined in claim 1, characterised in that the reactants have a linear velocity of between 0.5 and 2 cm/sec.
3. A method as defined in claim 1, characterised in that the temperature in the reactor or reactors ranges from 50 to 60°C.
4. A process as defined in claim 1, characterised in that said aliphatic alcohols are selected from the group consisting of methanol and ethanol.
5. A process as defined in claim 1, characterised in that two or more reactors are used in series.
6. A process as defined in claim 1, wherein the temperature in the reactor or reactors ranges from 50 to 55°C.
7. A process as defined in claim 2, wherein the temperature in the reactor or reactors ranges from 50 to 55°C.
8. A process as defined in claim 7, characterised in that said aliphatic alcohols are selected from the group consisting of methanol and ethanol.
9. A process as defined in claim 8, characterised in that two or more reactors are used in series.
10. A process as defined in claim 1, 2 or 3, characterised in that said reactors are provided with a macroporous acid ion exchange resin catalyst.
11. A process as defined in claim 4, 5 or 6, characterised in that said reactors are provided with a macroporous acid ion exchange resin catalyst.
12. A process as defined in claim 7, 8 or 9, characterised in that said reactors are provided with a macroporous acid ion exchange resin catalyst.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT20122A/82 | 1982-03-12 | ||
| IT20122/82A IT1150678B (en) | 1982-03-12 | 1982-03-12 | PROCEDURE FOR THE PRODUCTION OF TERBUTYL ALCHYL ETHERS IN THE PRESENCE OF BUTADIENE |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1205824A true CA1205824A (en) | 1986-06-10 |
Family
ID=11163984
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000421707A Expired CA1205824A (en) | 1982-03-12 | 1983-02-16 | Process for producing tert.butyl alkyl ethers in the presence of butadiene |
Country Status (33)
| Country | Link |
|---|---|
| JP (1) | JPS58167534A (en) |
| KR (1) | KR860001359B1 (en) |
| AT (1) | AT387959B (en) |
| AU (1) | AU559931B2 (en) |
| BE (1) | BE896127A (en) |
| BR (1) | BR8301020A (en) |
| CA (1) | CA1205824A (en) |
| CS (1) | CS232749B2 (en) |
| DD (1) | DD207194A5 (en) |
| DE (1) | DE3308736A1 (en) |
| DK (1) | DK65683A (en) |
| EG (1) | EG16276A (en) |
| ES (1) | ES8404670A1 (en) |
| FR (1) | FR2523121B1 (en) |
| GB (1) | GB2116546B (en) |
| GR (1) | GR78796B (en) |
| HU (1) | HU196351B (en) |
| IN (1) | IN159879B (en) |
| IT (1) | IT1150678B (en) |
| LU (1) | LU84665A1 (en) |
| MX (1) | MX155984A (en) |
| NL (1) | NL8300848A (en) |
| NO (1) | NO156606C (en) |
| NZ (1) | NZ203293A (en) |
| PH (1) | PH19851A (en) |
| PL (1) | PL140559B1 (en) |
| PT (1) | PT76375B (en) |
| RU (1) | RU1836318C (en) |
| SE (1) | SE461853B (en) |
| TR (1) | TR21654A (en) |
| YU (1) | YU49483A (en) |
| ZA (1) | ZA831152B (en) |
| ZM (1) | ZM1583A1 (en) |
Families Citing this family (24)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1190015B (en) * | 1986-05-27 | 1988-02-10 | Snam Progetti | PROCESS FOR THE PREPARATION OF ALCHYLTERBUTYL ETHERS |
| GB9027112D0 (en) * | 1990-12-13 | 1991-02-06 | British Petroleum Co Plc | Etherification |
| US7838708B2 (en) | 2001-06-20 | 2010-11-23 | Grt, Inc. | Hydrocarbon conversion process improvements |
| RU2366642C2 (en) | 2003-07-15 | 2009-09-10 | Джи Ар Ти, Инк. | Hydrocarbons synthesis |
| US20050171393A1 (en) | 2003-07-15 | 2005-08-04 | Lorkovic Ivan M. | Hydrocarbon synthesis |
| US8173851B2 (en) | 2004-04-16 | 2012-05-08 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons |
| US8642822B2 (en) | 2004-04-16 | 2014-02-04 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons using microchannel reactor |
| US7244867B2 (en) | 2004-04-16 | 2007-07-17 | Marathon Oil Company | Process for converting gaseous alkanes to liquid hydrocarbons |
| US7674941B2 (en) | 2004-04-16 | 2010-03-09 | Marathon Gtf Technology, Ltd. | Processes for converting gaseous alkanes to liquid hydrocarbons |
| US20060100469A1 (en) | 2004-04-16 | 2006-05-11 | Waycuilis John J | Process for converting gaseous alkanes to olefins and liquid hydrocarbons |
| US20080275284A1 (en) | 2004-04-16 | 2008-11-06 | Marathon Oil Company | Process for converting gaseous alkanes to liquid hydrocarbons |
| WO2007092410A2 (en) | 2006-02-03 | 2007-08-16 | Grt, Inc. | Separation of light gases from halogens |
| EP1993979A4 (en) | 2006-02-03 | 2011-07-06 | Grt Inc | Continuous process for converting natural gas to liquid hydrocarbons |
| US8921625B2 (en) | 2007-02-05 | 2014-12-30 | Reaction35, LLC | Continuous process for converting natural gas to liquid hydrocarbons |
| US7998438B2 (en) | 2007-05-24 | 2011-08-16 | Grt, Inc. | Zone reactor incorporating reversible hydrogen halide capture and release |
| US8282810B2 (en) | 2008-06-13 | 2012-10-09 | Marathon Gtf Technology, Ltd. | Bromine-based method and system for converting gaseous alkanes to liquid hydrocarbons using electrolysis for bromine recovery |
| US8198495B2 (en) | 2010-03-02 | 2012-06-12 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
| US8367884B2 (en) | 2010-03-02 | 2013-02-05 | Marathon Gtf Technology, Ltd. | Processes and systems for the staged synthesis of alkyl bromides |
| US8815050B2 (en) | 2011-03-22 | 2014-08-26 | Marathon Gtf Technology, Ltd. | Processes and systems for drying liquid bromine |
| US8436220B2 (en) | 2011-06-10 | 2013-05-07 | Marathon Gtf Technology, Ltd. | Processes and systems for demethanization of brominated hydrocarbons |
| US8829256B2 (en) | 2011-06-30 | 2014-09-09 | Gtc Technology Us, Llc | Processes and systems for fractionation of brominated hydrocarbons in the conversion of natural gas to liquid hydrocarbons |
| US8686211B2 (en) | 2011-09-07 | 2014-04-01 | Shell Oil Company | Process for preparing ethylene and/or propylene and a butadiene-enriched product |
| US8802908B2 (en) | 2011-10-21 | 2014-08-12 | Marathon Gtf Technology, Ltd. | Processes and systems for separate, parallel methane and higher alkanes' bromination |
| US9193641B2 (en) | 2011-12-16 | 2015-11-24 | Gtc Technology Us, Llc | Processes and systems for conversion of alkyl bromides to higher molecular weight hydrocarbons in circulating catalyst reactor-regenerator systems |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1224294B (en) * | 1961-01-09 | 1966-09-08 | Bayer Ag | Process for the production of tertiary butyl alkyl ethers |
| JPS4961109A (en) * | 1972-10-12 | 1974-06-13 | ||
| IT1012687B (en) * | 1974-05-21 | 1977-03-10 | Snam Progetti | PROCEDURE FOR THE SYNTHESIS OF ETHES RI ALCYL TER BUTYL FROM A PRIMARY ALCOHOL AND ISOBUTYLENE IN THE PRESENCE OF BUTADIENE |
| JPS5220963A (en) * | 1975-06-30 | 1977-02-17 | Daido Steel Co Ltd | Method of manufacturing precious metal powder |
| JPS5232241A (en) * | 1975-09-05 | 1977-03-11 | Fujitsu Ltd | Wireless data transmission system |
| FR2440931A1 (en) * | 1978-11-08 | 1980-06-06 | Inst Francais Du Petrole | PROCESS FOR PRODUCING ETHERS BY REACTION OF OLEFINS WITH ALCOHOLS |
| DE2928509A1 (en) * | 1979-07-14 | 1981-01-29 | Basf Ag | METHOD FOR THE SIMULTANEOUS PRODUCTION OF METHYL-TERT.-BUTYL ETHER AND PRODUCTION OF ISOBUTEN |
| JPS58146524A (en) * | 1982-02-25 | 1983-09-01 | Mitsubishi Gas Chem Co Inc | Preparation of tertiary ether |
-
1982
- 1982-03-12 IT IT20122/82A patent/IT1150678B/en active
-
1983
- 1983-02-15 NZ NZ203293A patent/NZ203293A/en unknown
- 1983-02-15 DK DK65683A patent/DK65683A/en not_active Application Discontinuation
- 1983-02-16 CA CA000421707A patent/CA1205824A/en not_active Expired
- 1983-02-18 GB GB08304536A patent/GB2116546B/en not_active Expired
- 1983-02-21 KR KR1019830000697A patent/KR860001359B1/en active IP Right Grant
- 1983-02-21 ZA ZA831152A patent/ZA831152B/en unknown
- 1983-02-22 AU AU11744/83A patent/AU559931B2/en not_active Expired - Fee Related
- 1983-02-23 GR GR70589A patent/GR78796B/el unknown
- 1983-02-24 PL PL1983240765A patent/PL140559B1/en unknown
- 1983-02-25 MX MX196394A patent/MX155984A/en unknown
- 1983-02-25 SE SE8301069A patent/SE461853B/en not_active IP Right Cessation
- 1983-02-25 LU LU84665A patent/LU84665A1/en unknown
- 1983-02-25 BR BR8301020A patent/BR8301020A/en unknown
- 1983-03-02 YU YU00494/83A patent/YU49483A/en unknown
- 1983-03-03 CS CS831493A patent/CS232749B2/en unknown
- 1983-03-04 NO NO830743A patent/NO156606C/en unknown
- 1983-03-07 ZM ZM15/83A patent/ZM1583A1/en unknown
- 1983-03-08 AT AT0080383A patent/AT387959B/en not_active IP Right Cessation
- 1983-03-08 PH PH28617A patent/PH19851A/en unknown
- 1983-03-09 TR TR21654A patent/TR21654A/en unknown
- 1983-03-09 NL NL8300848A patent/NL8300848A/en not_active Application Discontinuation
- 1983-03-10 BE BE0/210292A patent/BE896127A/en not_active IP Right Cessation
- 1983-03-11 ES ES520857A patent/ES8404670A1/en not_active Expired
- 1983-03-11 JP JP58039308A patent/JPS58167534A/en active Granted
- 1983-03-11 DE DE19833308736 patent/DE3308736A1/en active Granted
- 1983-03-11 IN IN302/CAL/83A patent/IN159879B/en unknown
- 1983-03-11 HU HU83846A patent/HU196351B/en unknown
- 1983-03-11 DD DD83248748A patent/DD207194A5/en not_active IP Right Cessation
- 1983-03-11 FR FR8304015A patent/FR2523121B1/en not_active Expired
- 1983-03-11 PT PT76375A patent/PT76375B/en unknown
- 1983-03-11 RU SU833560849A patent/RU1836318C/en active
- 1983-03-12 EG EG167/83A patent/EG16276A/en active
Also Published As
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
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