NO843022L - PROCEDURE FOR EXTRACTION OF PURE BUTEN-1 - Google Patents
PROCEDURE FOR EXTRACTION OF PURE BUTEN-1Info
- Publication number
- NO843022L NO843022L NO843022A NO843022A NO843022L NO 843022 L NO843022 L NO 843022L NO 843022 A NO843022 A NO 843022A NO 843022 A NO843022 A NO 843022A NO 843022 L NO843022 L NO 843022L
- Authority
- NO
- Norway
- Prior art keywords
- butene
- stream
- range
- atm
- abs
- Prior art date
Links
- 238000000605 extraction Methods 0.000 title 1
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 62
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 claims description 34
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 24
- 238000005984 hydrogenation reaction Methods 0.000 claims description 16
- 238000004821 distillation Methods 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 13
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 10
- 150000000475 acetylene derivatives Chemical class 0.000 claims description 8
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 7
- 150000001875 compounds Chemical class 0.000 claims description 6
- 238000006116 polymerization reaction Methods 0.000 claims description 6
- 239000001282 iso-butane Substances 0.000 claims description 5
- 238000009835 boiling Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 2
- 229920000642 polymer Polymers 0.000 claims 1
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000006317 isomerization reaction Methods 0.000 description 6
- IAQRGUVFOMOMEM-ONEGZZNKSA-N trans-but-2-ene Chemical compound C\C=C\C IAQRGUVFOMOMEM-ONEGZZNKSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 description 2
- -1 acetylene hydrocarbons Chemical class 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N ether Substances CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 description 2
- DNIAPMSPPWPWGF-GSVOUGTGSA-N (R)-(-)-Propylene glycol Chemical compound C[C@@H](O)CO DNIAPMSPPWPWGF-GSVOUGTGSA-N 0.000 description 1
- CHRJZRDFSQHIFI-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;styrene Chemical compound C=CC1=CC=CC=C1.C=CC1=CC=CC=C1C=C CHRJZRDFSQHIFI-UHFFFAOYSA-N 0.000 description 1
- YZUPZGFPHUVJKC-UHFFFAOYSA-N 1-bromo-2-methoxyethane Chemical compound COCCBr YZUPZGFPHUVJKC-UHFFFAOYSA-N 0.000 description 1
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000006266 etherification reaction Methods 0.000 description 1
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 239000002638 heterogeneous catalyst Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000000542 sulfonic acid group Chemical group 0.000 description 1
- 238000011282 treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/08—Alkenes with four carbon atoms
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treatment Of Liquids With Adsorbents In General (AREA)
- Extraction Or Liquid Replacement (AREA)
- Detergent Compositions (AREA)
Description
Foreliggende oppfinnelse vedrører en fremgangsmåte for utvinning av buten-1 med renhet egnet for polymerisering fra en fraksjon, fritt for isobuten eller hovedsakelig fritt for isobuten, omfattende trinnene med at man i en første destillasjonskolonne ved et trykk i området fra 5 til 20 abs. atm. destillerer den nevnte fraksjon under oppnåelse av en topp-strøm hovedsakelig inneholdende isobutan og en bunnstrøm inneholdende de resterende komponenter og at man desillerer strøm-men inneholdende de resterende komponenter i en annen destillasjonskolonne ved et trykk i området 3 til 10 abs. atm. under oppnåelse av en toppstrøm av buten-1 med renhet 80 til 95% og en bunnstrøm omfattende de høytkokende forbindelser n-butan og cis- og trans-buten-2 og det særegne ved fremgangsmåten i henhold til oppfinnelsen er at toppstrømmen fra den annen destillasjonskolonne føres til en selektiv hydrogeneringsenhet for butadien og de acetyleniske derivater idet disse forbindelser reduseres til en konsentrasjon i området fra 30 til 200 ppm idet strømmen som kommer fra den selektive hydrogeneringsenhet til slutt føres til en destillasjonskolonne som drives ved et trykk i området fra 3 til 10 abs. atm. hvor man fra en plate nær toppen av kolonnen oppnår buten-1 med renhet egnet for polymerisering . The present invention relates to a method for extracting butene-1 with a purity suitable for polymerization from a fraction, free of isobutene or mainly free of isobutene, comprising the steps that in a first distillation column at a pressure in the range from 5 to 20 abs. atm. distilling the said fraction while obtaining a top stream mainly containing isobutane and a bottom stream containing the remaining components and distilling the stream but containing the remaining components in another distillation column at a pressure in the range of 3 to 10 abs. atm. while obtaining a top stream of butene-1 with a purity of 80 to 95% and a bottom stream comprising the high-boiling compounds n-butane and cis- and trans-butene-2 and the peculiarity of the method according to the invention is that the top stream from the second distillation column is fed to a selective hydrogenation unit for butadiene and the acetylenic derivatives, these compounds being reduced to a concentration in the range from 30 to 200 ppm, the flow coming from the selective hydrogenation unit being finally fed to a distillation column operated at a pressure in the range from 3 to 10 abs. atm. where from a plate near the top of the column one obtains butene-1 with a purity suitable for polymerization.
Dise trekk ved oppfinnelsen fremgår av patentkravet.These features of the invention appear in the patent claim.
Buten-1 inneholdt i C^-hydrokarbonstrømmene består av vari-able prosentandeler av de følgende komponenter: buten-1, isobutan, isobuten, n-butan, buten^,^- og C,. —hydrokarboner av både mettet og olefin-karakter, butadien- og acetylen-derivater. The butene-1 contained in the C^-hydrocarbon streams consists of variable percentages of the following components: butene-1, isobutane, isobutene, n-butane, butene^,^- and C,. —hydrocarbons of both saturated and olefinic character, butadiene and acetylene derivatives.
De C^-hydrokarbonstrømmer som skal anvendes som råmaterialer ved fremgangsmåten i henhold til oppfinnelsen har et lavt innhold av butadien- og acetylen-derivater slik at hvis ut-gangsfraksjonen skriver seg fra en damp-crackingprosess må butadienet som inneholdes deri gi store prosentandeler fjernes ved hjelp av et løsningsmiddel eller ved en annen prosess. The C₁ hydrocarbon streams to be used as raw materials in the process according to the invention have a low content of butadiene and acetylene derivatives so that if the output fraction comes from a steam cracking process, the butadiene contained therein must be removed in large percentages by by means of a solvent or by another process.
Sammensetningen av de C^-hydrokarbonstrømmer som anvendes ved oppfinnelsen ligger innenfor de følgende grenser: The composition of the C2 hydrocarbon streams used in the invention lies within the following limits:
Det problem som må løses er utvinning av buten-1 idet man holder omdannelsen av buten-1 til buten-2 i trinnet med den selektive hydrogenering av butadienet og acetylen-derivatene så lav som mulig. The problem to be solved is the recovery of butene-1 while keeping the conversion of butene-1 to butene-2 in the step of the selective hydrogenation of the butadiene and acetylene derivatives as low as possible.
Den kjente teknikk lærer at den selektive hydrogenering av butadienet og acetylen-hydrokarbonene må gjennomføres før sep-areringstrinnene for de forskjellige komponenter fra buten-1, men når man arbeider ved hjelp av kjente prosesser opptrer sammen med hydrogenering også en ikke uvesentlig isomerisering av buten-1 til buten-2. The known technique teaches that the selective hydrogenation of the butadiene and the acetylene hydrocarbons must be carried out before the separation steps for the various components from butene-1, but when working with the aid of known processes, a not insignificant isomerization of butene also occurs together with hydrogenation. 1 to buten-2.
Graden av slik isomerisering avhenger av den mengde butadien som kan tillates i henhold til spesifikasjonene for buten-1. Jo lavere maksimalt innhold av butadien som tillates i henhold til spesifikasjonene for buten-1, dessto lavere må mengden av resterende butadien i C^-strømmen etter hydrogeneringen være og dessto høyere vil tapet av buten-1 være på grunn av isomeriseringen til buten-2. The degree of such isomerization depends on the amount of butadiene that can be allowed according to the specifications for butene-1. The lower the maximum content of butadiene allowed according to the specifications for butene-1, the lower must be the amount of residual butadiene in the C^ stream after the hydrogenation and the higher will be the loss of butene-1 due to the isomerization to butene-2 .
Som ren eksemplifisering, ved å gå ut fra et innhold av butadien i den strøm som føres til hydrogeneringstrinnet på omtrent 2%, hvis det maksimalt tillatte innhold av butadien i henhold til spesifikasjonene for buten-1 er 200 ppm er tapet av buten-1 på grunn av isomeriseringen omtrent 2 vekt% men hvis spesifikasjonene for buten-1 tillater et maksimalt innhold på 50 ppm butadien er isomeriseringstapet for buten-1 . høyere enn 5 vekt%. By way of example, assuming a content of butadiene in the stream fed to the hydrogenation step of approximately 2%, if the maximum content of butadiene allowed according to the specifications for butene-1 is 200 ppm, the loss of butene-1 is due to the isomerization approximately 2% by weight but if the specifications for butene-1 allow a maximum content of 50 ppm butadiene, the isomerization loss for butene-1 is . higher than 5% by weight.
Det er nå overraskende funnet at det er mulig å redusere ulem-pene med den tidligere kjente teknikk ved å anvende et selek-tivt hydrogeneringstrinn for butadienet og acetylenderivatene anordnet i et passende punkt av anlegget. It has now surprisingly been found that it is possible to reduce the disadvantages of the previously known technique by using a selective hydrogenation step for the butadiene and the acetylene derivatives arranged in a suitable point of the plant.
C^-strømmen underkastes de konvensjonelle behandlinger for separering av butenet ved hjelp av omdannelse av isobutenet til en alkyl-tert-butyl eter ved omsetning med en alifatisk alkohol, foretrukket metanol, i nærvær av en heterogen kata-lysator med funksjonelle sulfonsyregrupper på en styren-di-vinylbenzen-grunnmasse, spesielt av typen "Amberlyst 15". The C 2 stream is subjected to the conventional treatments for separating the butene by converting the isobutene to an alkyl-tert-butyl ether by reaction with an aliphatic alcohol, preferably methanol, in the presence of a heterogeneous catalyst with functional sulfonic acid groups on a styrene -di-vinylbenzene base material, especially of the "Amberlyst 15" type.
Ved hjelp av de beskrevne reaksjoner omdannes praktisk alt isobutenet til en alkyl-tert-butyl eter som i sin tur fjernes ved destillasjon på kjent måte. By means of the described reactions, practically all of the isobutene is converted into an alkyl-tert-butyl ether, which in turn is removed by distillation in a known manner.
Fremgangsmåten i henhold til oppfinnelsen omfatter således trinnene med at man i en første destillasjonskolonne som drives ved et trykk i området fra 5 til 20 abs. atm. destillerer C^-fraksjonen inneholdende de tidligere angitte komponenter, fri for isobuten eller hovedsakelig fri for isobuten, under oppnåelse av en toppstrøm hovedsakelig bestående av isobutan og en bunnstrøm bestående av de resterende komponenter og som i sin tur destilleres i en annen destillasjonskolonne ved et trykk på mellom 3 og 10 abs. atm. under oppnåelse av en toppstrøm bestående av buten-1 med en renhetsgrad i området fra 80 til 95% (inneholdende buten-1 + funda-mentalt butan og butadien- + acetylen-derivater) og en bunn-strøm inneholdende høytkokende forbindelser, n-butan og cis-og trans-buten-2. The method according to the invention thus comprises the steps in which, in a first distillation column which is operated at a pressure in the range from 5 to 20 abs. atm. distills the C^ fraction containing the previously indicated components, free of isobutene or substantially free of isobutene, obtaining an overhead stream consisting mainly of isobutane and a bottom stream consisting of the remaining components and which in turn is distilled in another distillation column at a pressure of between 3 and 10 abs. atm. while obtaining a top stream consisting of butene-1 with a degree of purity in the range from 80 to 95% (containing butene-1 + fundamental butane and butadiene + acetylene derivatives) and a bottom stream containing high-boiling compounds, n-butane and cis- and trans-butene-2.
Toppstrømmen fra den annen destillasjonskolonne føres til en selektiv hydrogeneringsenhet for butadien- og The top stream from the second distillation column is fed to a selective hydrogenation unit for butadiene and
acetylen-derivatene hvor konsentrasjonen av de nevnte forbindelser reduseres til en verdi i området 30 til 200 ppm for å oppfylle spesifikasjonene for buten-1 med polymerisasjons-renhetsgrad. the acetylene derivatives where the concentration of said compounds is reduced to a value in the range of 30 to 200 ppm in order to meet the specifications for butene-1 with polymerization purity.
Hydrogeneringsenheten drives under de følgende betingelser: innløpstemperatur 35 til 50°C og arbeidstrykk 4 til 20 abs. atm . The hydrogenation unit is operated under the following conditions: inlet temperature 35 to 50°C and working pressure 4 to 20 abs. atm.
Strømmen som kommer fra den selektive hydrogeneringsenhet som er berøvet dienforbindelser og acetylenforbindelser, føres til en destillasjonskolonne som drives ved et trykket i området fra 3 til 10 abs. atm. og hvor man fra en plate nær toppen av kolonnen oppnår buten-1 med polymerisasjons-renhetsgrad og som bunnstrøm n-butan og buten-2 med reduserte mengder av buten-1. The stream coming from the selective hydrogenation unit deprived of diene compounds and acetylene compounds is fed to a distillation column operated at a pressure in the range from 3 to 10 abs. atm. and where one obtains from a plate near the top of the column butene-1 with polymerization purity and as bottom stream n-butane and butene-2 with reduced amounts of butene-1.
Fremgangsmåten i henhold til oppfinnelsen opprettholder sine fordeler med bare å kreve milde reaksjonsbetingelser også når den selektive hydrogenering gjennomføres i nærvær av inhibi-torer for bindings-isomerisering fra buten-1 til buten-2 og som er tilsatt C^-fraksjonen. The method according to the invention maintains its advantages of only requiring mild reaction conditions also when the selective hydrogenation is carried out in the presence of inhibitors for bond isomerization from butene-1 to butene-2 and which are added to the C₂ fraction.
Fremgangsmåten i henhold til den foreliggende oppfinnelse har i alle fall den ytterligere fordel med å tillate reduserte dimensjoner for utstyret nødvendig for den selektive hydrogenering og derav følgende reduserte anleggsomkostninger. The method according to the present invention in any case has the further advantage of allowing reduced dimensions for the equipment necessary for the selective hydrogenation and consequently reduced construction costs.
Vedrørende typene av komponenter i de forskjellige strømmer vises til det etterfølgende eksempel som illustrerer eksempel-vise konsentrasjoner av de forskjellige komponenter i de enk-elte strømmer og arbeidstrykkene i de forskjellige trinn. Regarding the types of components in the different streams, reference is made to the following example which illustrates exemplary concentrations of the different components in the individual streams and the working pressures in the different stages.
EksempelExample
Dette eksempel ble gjennomført i samsvar med den skjematiske illustrasjon i den vedføyde tegning hvori (1) er C^-strømmen omfattende blant annet buten-1, isobuten, butadien- og acetylen-derivater, (2) er en metanolstrøm som tilføres for-etringsenheten (16) for isobuten, (3) er strømmen av metyl-tert-butyl eter som dannes, (4) er strømmen hovedsakelig fri for isobuten, (18) er den første destillasjonskolonne som drives med omtrent 14 abs. atm., (5) er toppstrømmen hovedsakelig omfattende isobutan, (6) er reststrømmen som føres til den annen destillasjonskolonne (19) som drives ved et trykk på omtrent 6 abs. atm. (7) er en strøm hovedsakelig inneholdende buten-1, (8) er en strøm inneholdende de tunge produkter. Strømmen (7) tilføres hydrogeneringsenheten (17) hvortil hydrogen tilføres gjennom ledningen (9) og hvorfra strømmen (11) tas ut hovedsakelig bestående av overskuddshydrogen og buten-1, (10) er den hydrogenerte strøm som føres til frak-sjoneringskolonnen (20) som drives ved et trykk på omtrent 7 abs. atm. og fra toppen av denne oppnås en strøm (12) bestående av ukondenserbare substanser og buten-1 idet det fra den 10. plate fra toppen oppnås en strøm (13) av buten-1 med poly-merisas jons-renhetsgrad og fra bunnen oppnås resten (14) hovedsakelig bestående av n-butan og buten-2 . This example was carried out in accordance with the schematic illustration in the attached drawing in which (1) the C^ stream comprises, among other things, butene-1, isobutene, butadiene and acetylene derivatives, (2) is a methanol stream fed to the etherification unit (16) for isobutene, (3) is the stream of methyl tert-butyl ether formed, (4) is the stream essentially free of isobutene, (18) is the first distillation column operated at about 14 abs. atm., (5) is the overhead stream mainly comprising isobutane, (6) is the residual stream which is fed to the second distillation column (19) which is operated at a pressure of about 6 abs. atm. (7) is a stream mainly containing butene-1, (8) is a stream containing the heavy products. The stream (7) is supplied to the hydrogenation unit (17) to which hydrogen is supplied through the line (9) and from which the stream (11) consisting mainly of excess hydrogen and butene-1 is withdrawn, (10) is the hydrogenated stream which is fed to the fractionation column (20) which is operated at a pressure of about 7 abs. atm. and from the top of this, a stream (12) consisting of non-condensable substances and butene-1 is obtained, as from the 10th plate from the top, a stream (13) of butene-1 with polymerization ion purity is obtained and from the bottom, the rest is obtained (14) mainly consisting of n-butane and butene-2.
Strømmen (15) er summen av strømmen (5), (8) og (14). The current (15) is the sum of the currents (5), (8) and (14).
Materialbalansen ved prosessen fremgår av den etterfølgende tabell hvor posisjons-tallangivelsene refererer til figuren. The material balance for the process appears in the following table where the position figures refer to the figure.
Claims (1)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT22294/83A IT1194351B (en) | 1983-07-28 | 1983-07-28 | PROCEDURE FOR THE RECOVERY OF BUTENE-1 DEGREE POLYMERIZATION |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO843022L true NO843022L (en) | 1985-01-29 |
Family
ID=11194295
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO843022A NO843022L (en) | 1983-07-28 | 1984-07-25 | PROCEDURE FOR EXTRACTION OF PURE BUTEN-1 |
Country Status (26)
| Country | Link |
|---|---|
| JP (1) | JPS6051131A (en) |
| KR (1) | KR870000583B1 (en) |
| AU (1) | AU561302B2 (en) |
| BE (1) | BE900248A (en) |
| BR (1) | BR8403665A (en) |
| CA (1) | CA1232919A (en) |
| CS (1) | CS250667B2 (en) |
| DD (1) | DD222000A5 (en) |
| DE (1) | DE3426349A1 (en) |
| DK (1) | DK369484A (en) |
| ES (1) | ES8507007A1 (en) |
| FR (1) | FR2549825B1 (en) |
| GB (1) | GB2144146B (en) |
| GR (1) | GR82261B (en) |
| HU (1) | HUT36762A (en) |
| IT (1) | IT1194351B (en) |
| LU (1) | LU85466A1 (en) |
| NL (1) | NL8402384A (en) |
| NO (1) | NO843022L (en) |
| PL (1) | PL248948A1 (en) |
| PT (1) | PT78990B (en) |
| RO (1) | RO90623A (en) |
| SE (1) | SE8403426L (en) |
| TR (1) | TR22082A (en) |
| YU (1) | YU132184A (en) |
| ZA (1) | ZA845088B (en) |
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|---|---|---|---|---|
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Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1280845B (en) * | 1965-10-29 | 1968-10-24 | Huels Chemische Werke Ag | Process for the selective hydrogenation of butadiene- (1,3) in a C-hydrocarbon mixture containing larger amounts of 1-butene and small amounts of butadiene- (1, 3) |
| FR2474024A1 (en) * | 1980-01-23 | 1981-07-24 | Inst Francais Du Petrole | PROCESS FOR PRODUCING BUTENE-1 FROM A C4 CUTTING OF HYDROCARBONS |
| FR2493306A1 (en) * | 1980-10-30 | 1982-05-07 | Inst Francais Du Petrole | High-purity 1-butene recovery from mixed butene streams - by isobutene polymerisation to gasoline and fractionation |
| FR2495605A1 (en) * | 1980-12-05 | 1982-06-11 | Inst Francais Du Petrole | High-purity butene-1 isolated from steam cracker butene(s) - by conversion of isobutene to methyl tert. butyl ether and fractionation |
| FR2508437A1 (en) * | 1981-06-26 | 1982-12-31 | Inst Francais Du Petrole | Steam-cracker butene(s) cut upgraded to pure butene-1, gasoline - and opt. jet fuel via initial polymerisation-dismutation on acid catalyst |
| US4820472A (en) * | 1981-07-14 | 1989-04-11 | Westinghouse Electric Corp. | Nuclear reactor spent fuel storage rack |
-
1983
- 1983-07-28 IT IT22294/83A patent/IT1194351B/en active
-
1984
- 1984-06-27 SE SE8403426A patent/SE8403426L/en not_active Application Discontinuation
- 1984-07-03 ZA ZA845088A patent/ZA845088B/en unknown
- 1984-07-04 GR GR75186A patent/GR82261B/el unknown
- 1984-07-05 CS CS845243A patent/CS250667B2/en unknown
- 1984-07-06 GB GB08417309A patent/GB2144146B/en not_active Expired
- 1984-07-16 LU LU85466A patent/LU85466A1/en unknown
- 1984-07-17 DE DE19843426349 patent/DE3426349A1/en not_active Ceased
- 1984-07-19 BR BR8403665A patent/BR8403665A/en unknown
- 1984-07-23 KR KR1019840004354A patent/KR870000583B1/en active IP Right Grant
- 1984-07-23 AU AU30960/84A patent/AU561302B2/en not_active Expired - Fee Related
- 1984-07-24 CA CA000459574A patent/CA1232919A/en not_active Expired
- 1984-07-25 NO NO843022A patent/NO843022L/en unknown
- 1984-07-25 TR TR22082A patent/TR22082A/en unknown
- 1984-07-26 YU YU01321/84A patent/YU132184A/en unknown
- 1984-07-26 PL PL24894884A patent/PL248948A1/en unknown
- 1984-07-26 FR FR8411913A patent/FR2549825B1/en not_active Expired
- 1984-07-27 DD DD84265727A patent/DD222000A5/en unknown
- 1984-07-27 PT PT78990A patent/PT78990B/en unknown
- 1984-07-27 ES ES534969A patent/ES8507007A1/en not_active Expired
- 1984-07-27 BE BE0/213405A patent/BE900248A/en not_active IP Right Cessation
- 1984-07-27 RO RO84115361A patent/RO90623A/en unknown
- 1984-07-27 DK DK369484A patent/DK369484A/en not_active Application Discontinuation
- 1984-07-27 JP JP59155719A patent/JPS6051131A/en active Pending
- 1984-07-27 HU HU842900A patent/HUT36762A/en unknown
- 1984-07-30 NL NL8402384A patent/NL8402384A/en not_active Application Discontinuation
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