EP2802637A1 - Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif - Google Patents

Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif

Info

Publication number
EP2802637A1
EP2802637A1 EP13700159.0A EP13700159A EP2802637A1 EP 2802637 A1 EP2802637 A1 EP 2802637A1 EP 13700159 A EP13700159 A EP 13700159A EP 2802637 A1 EP2802637 A1 EP 2802637A1
Authority
EP
European Patent Office
Prior art keywords
crude
cut
hydrocarbons
stripping column
purified
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
Application number
EP13700159.0A
Other languages
German (de)
English (en)
Other versions
EP2802637B1 (fr
Inventor
Bernd Heida
Randolf Hugo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Priority to EP13700159.0A priority Critical patent/EP2802637B1/fr
Publication of EP2802637A1 publication Critical patent/EP2802637A1/fr
Application granted granted Critical
Publication of EP2802637B1 publication Critical patent/EP2802637B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent
    • 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
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/12—Liquefied petroleum gas

Definitions

  • the invention relates to a method for providing a vaporized purified R0h- C4- Thomase.es as feed stream for an extractive distillation with a selective solvent.
  • C 4 cut denotes mixtures of hydrocarbons having predominantly 4 carbon atoms per molecule.
  • C 4 cuts are obtained, for example, in the production of ethylene and / or propylene by thermal cracking, usually in steam crackers, especially naphtha crackers or fluidized catalytic cracking (FCC) crackers of a petroleum fraction, such as liquefied petroleum gas, light gasoline or gas oil. Furthermore, C 4 cuts are obtained in the catalytic dehydrogenation of n-butane and / or n-butene.
  • C 4 cuts generally contain butanes, butenes, 1,3-butadiene, small amounts of C 3 and C 4 acetylenes, 1,2-butadiene and C 5+ hydrocarbons.
  • the separation of C 4 cuts is a complicated distillation problem because of the small differences in the relative volatilities of the components. Therefore, the separation is carried out by a so-called extractive distillation, ie a distillation with the addition of a selective solvent (also referred to as extractant), which has a higher boiling point than the mixture to be separated and which increases the differences in the relative volatilities of the components to be separated.
  • Crude C 4 sections contain impurities which would lead to problems in the extractive distillation, in particular foaming of the solvent and apparatus fouling, so that they must be separated just before the supply of R0h- C4- section for extractive distillation to a ensure reliable operation of the extractive distillation.
  • Impurities leading to the above problems are particularly high relative to 1,3-butadiene higher boiling components, especially C 5+ hydrocarbons (predominantly hydrocarbons having 5 or more carbon atoms per molecule, isoprene, C 4 oligomers and polymers, ie Oligomers and optionally polymers of butadiene of the formula (C 4 H 6 ) n, where n is greater than or equal to 2.
  • the proportion of C 5+ hydrocarbons in C 4 cuts is dependent in particular on the operating conditions during thermal cracking and is up to to 1000 ppm by weight or even up to 5000 ppm by weight, in individual cases up to 1 wt .-%, based on the total weight of R0h-C4-Schnitt.es.
  • the C 4 oligomers and polymers are formed in particular by storage and transport, their proportion is therefore largely dependent on the storage and transport conditions, in particular temperature, duration, inerting of the atmosphere under which the storage and / or transport takes place.
  • C 3 hydrocarbons ie hydrocarbons having three carbon atoms per molecule
  • the extractive distillation can cause problems; These are in particular methylacetylene, which has a similar affinity to the commonly used selective solvents such as 1, 3-butadiene.
  • the proportion of C 3 hydrocarbons should therefore be limited in the feed stream for extractive distillation to a maximum of 50 ppm by weight, based on the total weight of the feed stream.
  • the bottom stream is then fed to an evaporator vessel for the purpose of separating the high-boiling components from 1,3-butadiene, ie an apparatus with a single separation stage.
  • the depleted with C 3 components crude C 4 stream is almost completely evaporated, and indeed flow controlled, so that compared to 1, 3-butadiene high-boiling components in the remaining liquid content not above 5 wt .-%, in particular not above 1 wt .-%, or even not more than 0.1 wt .-%, based on the total weight of the crude boiler supplied to the evaporator C 4 - Thomases lie.
  • the liquid stream remaining in the evaporator vessel is discharged as purge stream.
  • the disadvantage here however, that high levels of recyclables, C 4 hydrocarbons are discharged via the purge stream together with the high boilers.
  • This object is achieved by a method of providing a vapor purified crude C 4 fraction as a feed stream for an extractive distillation using a selective solvent, starting from a crude liquid C 4 fraction as a feed stream containing, in addition butanes, butenes and 1, 3 Butadiene C 3 hydrocarbons, C 4 oligomers and polymers, and C 5+ hydrocarbons, wherein the purified crude vapor C 4 - cut less than two-thirds of the C 5+ hydrocarbons contained in the feed stream and less than 5 wt .-% of the feed stream contained in the C 4 oligomers and polymers containing the process steps
  • a stripping column to the evaporator boiler, that is to provide evaporator boiler and stripping column as separate apparatuses.
  • Evaporator boilers are known in the process engineering simple apparatus. They usually include a boiler, in which a gas phase can separate from a liquid phase, and a heat exchanger, which is located inside or outside the boiler.
  • a stripping column is assigned to the evaporator vessel. Since the stripping column and the evaporator boiler is intended only for depletion of high boilers, it is possible to operate the stripping column in a simple manner, without a condenser at the top of the column.
  • a typical crude C 4 cut from a naphtha cracker has the following composition in weight percent:
  • Raw C 4 cuts from naphtha crackers thus contain predominantly butanes, butenes and 1, 3-butadiene. In addition, small amounts of other hydrocarbons are included. C 4 -acetylenes are frequently present in a proportion of 5% by weight or even up to 2% by weight.
  • suitable substances generally include substances or mixtures which have a higher boiling point than the mixture to be separated and a greater affinity for conjugated double bonds and triple bonds than simple double bonds and single bonds, preferably dipolar, particularly preferably dipolar, aprotic solvents , For technical reasons, less or non-corrosive substances are preferred.
  • Suitable selective solvents for the process according to the invention are, for example, butyrolactone, nitriles such as acetonitrile, propionitrile, methoxypropionitrile, ketones such as acetone, furfurol, N-alkyl-substituted lower aliphatic acid amides such as dimethylformamide, diethylformamide, dimethylacetamide, diethylacetamide, N-formylmorpholine, N-alkyl-substituted cydic acid amides (Lactams) such as N-alkylpyrrolidones, in particular N-methylpyrrolidone.
  • nitriles such as acetonitrile, propionitrile, methoxypropionitrile
  • ketones such as acetone, furfurol
  • N-alkyl-substituted lower aliphatic acid amides such as dimethylformamide, diethylformamide, dimethylacetamide, die
  • N-alkyl substituted lower aliphatic acid amides or N-alkyl substituted cydic acid amides are used. Particularly advantageous are dimethylformamide, acetonitrile, furfurol and in particular N-methylpyrrolidone.
  • mixtures of these solvents with one another for example N-methylpyrrolidone with acetonitrile
  • mixtures of these solvents with cosolvents such as water and / or tert-butyl ether, for example methyl tert-butyl ether, ethyl tert-butyl ether, propyl tert-butyl ether, n- or iso-butyl tert-butyl ether can be used.
  • N-methylpyrrolidone preferably in aqueous solution, in particular with 8 to 10 wt .-% water, particularly preferably with 8.3 wt .-% water.
  • N-methylpyrrolidone preferably in aqueous solution, in particular with 8 to 10 wt .-% water, particularly preferably with 8.3 wt .-% water.
  • it should be fed as a feed stream, a purified vaporized crude C 4 cut less than 50 Ppm by weight of C 3 hydrocarbons, based on the total weight of the purified vaporous R0h-C4 cut, less than two-thirds of the C 5+ hydrocarbons contained in the feed stream and less than 5% by weight of the C contained in the feed stream 4 -oligomers and polymers.
  • the C 3 hydrocarbons in the gaseous purified crude C 4 - cut to less than 10 ppm by weight, based on the total weight of the gaseous purified R0h- C4- Thomase.es, or even more preferably less than 4 wt. -ppm, depleted in a distillation column upstream of the evaporator boiler.
  • the C 5+ hydrocarbons are depleted in the gaseous purified crude C 4 cut to less than half of the C 5+ hydrocarbons present in the feed stream.
  • the stripping column is preferably operated at a top pressure in the range of 3 to 7 bar absolute, more preferably at a top pressure in the range of 4.5 to 5.5 bar absolute.
  • the stripping column has in particular 1 to 15 theoretical plates.
  • 1 is a schematic representation of the evaporator boiler with attached stripping column
  • Fig. 2 is a schematic representation of an evaporator boiler with associated stripping column.
  • the schematic representation in Fig. 1 shows an evaporator vessel, VK, at the upper end of which a stripping column K connects, such that the Evaporator VK and the stripping column K form a single apparatus.
  • a sump evaporator is provided at the lower end of the evaporator vessel VK .
  • the stripping column K is supplied in the upper region thereof the liquid crude C 4 cut as stream 1, and at the top of the stripping column K, the purified crude C 4 - cut, stream 2, deducted.
  • Fig. 2 shows the schematic representation of a further preferred embodiment, in which the evaporator vessel VK and the stripping column K are formed as separate apparatus, and wherein a direct gas and liquid exchange at the upper end of the evaporator vessel VK is provided with the stripping column K.
  • the evaporator boiler VK is equipped with a sump evaporator S.
  • the stripping column K is fed in the upper region thereof the liquid C 4 cut as stream 1 and withdrawn as overhead stream of the vaporized purified crude C 4 cut , stream 2.
  • the starting point is a crude liquid C 4 cut as feed stream for a 100 kt / year plant containing 200 ppm of propane, 400 ppm of propene, 300 ppm of propadiene, 400 ppm of propyne, 2.0% of n-butane, 6.0 % isobutane, 19.0% n-butene, 28.3% isobutene, 5.5% trans-2-butene, 4.4% cis-2-butene, 39.0% butadiene-1, 3 , 0.2% butadiene-1, 2, 1200 ppm butyn-1, 4500 ppm vinyl acetylene and 1000 ppm iso-pentane, 3-methylbutene-1 and 2-methylbutene-2, in each case based on the total weight of the feed stream.
  • C 4 oligomers and polymers can be contained in the% range.
  • the above crude C 4 cut is subjected to a pre-purification, for comparison in a plant with a distillation column in which the C 3 hydrocarbons are removed overhead and the remaining components are withdrawn via the bottom whereupon the bottoms stream is fed to an evaporator vessel for separation of the high boiling components relative to 1,3-butadiene, ie a single separation apparatus.
  • the crude C 4 stream depleted in C 3 components is virtually completely vaporized and discharged under flow control, so that the C 5 components which boil over 1, 3-butadiene in the remaining liquid fraction do not exceed 5% by weight, based on the total weight of the R0h- C4-Schnitten.es supplied to the evaporator vessel, lie to the loss of C 4 components in liquid residue to keep small.
  • the proportion of oligomers and polymers contained in the liquid residue is significantly greater because of the lower vapor pressure.
  • the liquid stream remaining in the evaporator vessel is discharged as purge stream.
  • the same crude C 4 cut is fed as feed stream to an evaporator vessel VK, on which a stripping column K is set up with 5 theoretical plates, to which the liquid C 4 cut 1 is fed in the upper region and from the top End of the same is withdrawn from the gaseous purified crude C 4 cut 2, wherein the stripping column K is operated without a condenser at the top of the column.
  • a stripping column K is set up with 5 theoretical plates, to which the liquid C 4 cut 1 is fed in the upper region and from the top End of the same is withdrawn from the gaseous purified crude C 4 cut 2, wherein the stripping column K is operated without a condenser at the top of the column.
  • the residue stream (from the evaporator vessel) is according to the prior art 160 kg / h, with a proportion of 1, 3-butadiene of 38.6 wt .-%.
  • a purified crude C 4 cut with a higher degree of purity, compared to the method of the prior art is separated by the novel process.
  • ppm C 5 components additional proportions of C 6 components as well as oligomers and polymers, which are not taken into consideration here, may be used
  • 94.16 kg / h C 5 - fed components according to the prior art extractive distillation In the case according to the invention, on the other hand, only 55.1 kg / h of C 5 components of the extractive distillation are fed in.
  • the loss of desired product 1, 3-butadiene is thus greater by about 192 t / year in the process according to the prior art than in the process according to the invention.
  • the solvent forming a closed circuit the previous separation of interfering components and impurities keeps the same clean, thereby minimizing the regeneration effort.
  • the contamination of the extractive distillation unit (fouling of the beds in the columns) and foaming are kept low. As a result, less antifoam is required with correspondingly lower costs.
  • Reduced fouling reduces the cleaning effort for a shutdown. Each shutdown means a production loss of about 2 weeks; this adds to the cleaning effort. This leads to costs in the 7-digit range.

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)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé d'obtention d'une fraction C4 brute purifiée (2) sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif afin de produire du 1,3-butadiène brut à partir d'une fraction C4 brute liquide (1) en tant que charge de départ contenant, outre des butanes, des butènes et du 1,3-butadiène, des hydrocarbures C3, des oligomères et polymères C4 ainsi que des hydrocarbures C5+. Ce procédé comprend les étapes suivantes : 1) la séparation des oligomères et polymères C4 ainsi que des hydrocarbures C5+, respectivement jusqu'à atteindre les teneurs résiduelles indiquées plus haut pour la fraction C4 brute purifiée sous forme de vapeur ; et 2) la vaporisation de la fraction C4 brute liquide dans une chaudière de vaporisation (VK). Le procédé est caractérisé en ce que la chaudière de vaporisation (VK) est associée à une colonne de rectification (K) comprenant un ou plusieurs étages de séparation. La fraction C4 liquide (1) est amenée à la partie supérieure de la colonne de rectification. La colonne est en liaison directe d'échange de gaz et de liquide avec la chaudière de vaporisation (VK) dans sa partie inférieure. La fraction C4 brute purifiée (2) est soutirée à la partie supérieure de la colonne de rectification (K), cette dernière fonctionnant sans condenseur de tête.
EP13700159.0A 2012-01-11 2013-01-10 Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif Active EP2802637B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP13700159.0A EP2802637B1 (fr) 2012-01-11 2013-01-10 Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP12150824 2012-01-11
EP13700159.0A EP2802637B1 (fr) 2012-01-11 2013-01-10 Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif
PCT/EP2013/050366 WO2013104692A1 (fr) 2012-01-11 2013-01-10 Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif

Publications (2)

Publication Number Publication Date
EP2802637A1 true EP2802637A1 (fr) 2014-11-19
EP2802637B1 EP2802637B1 (fr) 2017-03-22

Family

ID=47553075

Family Applications (1)

Application Number Title Priority Date Filing Date
EP13700159.0A Active EP2802637B1 (fr) 2012-01-11 2013-01-10 Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif

Country Status (5)

Country Link
EP (1) EP2802637B1 (fr)
JP (1) JP6067748B2 (fr)
KR (1) KR102049312B1 (fr)
CN (1) CN104053752B (fr)
WO (1) WO2013104692A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3793969A1 (fr) 2018-05-18 2021-03-24 SABIC Global Technologies B.V. Procédé de production d'un additif de carburant par une unité d'hydratation

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2877173A (en) * 1955-03-23 1959-03-10 Standard Oil Co Hydroforming process
US4419188A (en) * 1980-06-02 1983-12-06 Mccall Thomas F Thermally coupled extractive distillation process
JPS58167683A (ja) * 1982-03-29 1983-10-03 Nippon Zeon Co Ltd 抽出蒸留方法
DE10022465A1 (de) * 2000-05-09 2001-11-15 Basf Ag Verfahren und Vorrichtung zur Aufarbeitung eines C4-Schnitts aus der Fraktionierung von Erdöl
DE10333756A1 (de) * 2003-07-24 2005-02-17 Basf Ag Verfahren zur Auftrennung eines Roh-C4-Schnittes
DE102004005930A1 (de) * 2004-02-06 2005-08-25 Basf Ag Verfahren zur Gewinnung von Roh-1,3-Butadien
US8840707B2 (en) * 2004-07-06 2014-09-23 Fluor Technologies Corporation Configurations and methods for gas condensate separation from high-pressure hydrocarbon mixtures
JP5074489B2 (ja) * 2006-07-12 2012-11-14 ビーエーエスエフ ソシエタス・ヨーロピア 選択的溶剤を用いる抽出蒸留によるｃ４カットの分離のための方法
CN101492335B (zh) * 2008-01-23 2013-07-31 中国石油化工股份有限公司 综合利用混合碳四的组合方法

Also Published As

Publication number Publication date
JP6067748B2 (ja) 2017-01-25
KR20140120329A (ko) 2014-10-13
JP2015508409A (ja) 2015-03-19
CN104053752A (zh) 2014-09-17
KR102049312B1 (ko) 2019-11-28
EP2802637B1 (fr) 2017-03-22
WO2013104692A1 (fr) 2013-07-18
CN104053752B (zh) 2016-08-31

Similar Documents

Publication Publication Date Title
EP2043977B1 (fr) Procede de separation d'une fraction en c4 par distillation extractive avec un solvant selectif
EP1718585B1 (fr) Procede pour recuperer du 1,3-butadiene brut
DE1568902C3 (de) VRFAHREN ZUR Abtrennung von 13-Butadien, Isopren und 13-Pentadien aus einer C4 - oder C5 -Kohlenwasserstoffmischung
EP1501773B1 (fr) Procede pour produire du butene en continu a partir d'une fraction c sb 4 /sb
DE2724365A1 (de) Verfahren zum trennen eines c tief 4 -kohlenwasserstoffgemisches durch extraktive destillation
EP1628940B1 (fr) Procede d'extraction de 1,3-butadiene brut a partir d'une fraction de c4
DE102010011014A1 (de) Verfahren und Vorrichtung zur destillativen Gewinnung von Rein-1,3-Butadien aus Roh-1,3-Butadien
EP1656334B1 (fr) Procede pour decomposer une coupe c sb 4 /sb brute
EP2788457B1 (fr) Procédé de distillation extractive au moyen d'un solvant sélectif utilisant une fraction c4 brute purifiée sous forme de vapeur en tant que flux de départ
DE2911395C2 (de) Verfahren zur Gewinnung eines konjugierten Diolefins aus einem C↓4↓- oder C↓5↓-Kohlenwasserstoffgemisch
EP0284971B1 (fr) Procédé pour la production de 1,3-butadiène
EP1530555A1 (fr) Procede pour retraiter du 1,3-butadiene brut
EP2496539B1 (fr) Procédé de séparation d'une coupe c4 par distillation extractive avec un solvant sélectif
EP2802637B1 (fr) Procédé d'obtention d'une fraction c4 brute purifiée sous forme de vapeur en tant que courant de départ d'une distillation extractive au moyen d'un solvant sélectif
DE3339157A1 (de) Verfahren zur gewinnung eines konjugierten diolefins und/oder olefins aus einem c(pfeil abwaerts)4(pfeil abwaerts)- oder c(pfeil abwaerts)5(pfeil abwaerts)-kohlenwasserstoffgemisch
EP3573943B1 (fr) Procédé d'obtention de 1,3-butadiène pur
EP3596033B1 (fr) Procédé simplifié d'obtention de 1,3-butadiène pur
WO2019007781A1 (fr) Procédé et système pour séparer des hydrocarbures c4 par distillation extractive
DE3346695A1 (de) Verfahren zur trennung eines c(pfeil abwaerts)4(pfeil abwaerts)-kohlenwasserstoffgemisches durch extraktivdestillation
DE2911393B1 (de) Verfahren zur Gewinnung eines konjugierten Diolefins aus einem C4- oder C5-Kohlenwasserstoffgemisch
DE2911396C2 (de) Verfahren zur Gewinnung eines konjugierten Diolefins aus einem C↓4↓- oder C↓5↓-Kohlenwasserstoffgemisch

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

17P Request for examination filed

Effective date: 20140811

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

DAX Request for extension of the european patent (deleted)
GRAP Despatch of communication of intention to grant a patent

Free format text: ORIGINAL CODE: EPIDOSNIGR1

INTG Intention to grant announced

Effective date: 20161208

GRAS Grant fee paid

Free format text: ORIGINAL CODE: EPIDOSNIGR3

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

REG Reference to a national code

Ref country code: GB

Ref legal event code: FG4D

Free format text: NOT ENGLISH

REG Reference to a national code

Ref country code: CH

Ref legal event code: EP

REG Reference to a national code

Ref country code: AT

Ref legal event code: REF

Ref document number: 877769

Country of ref document: AT

Kind code of ref document: T

Effective date: 20170415

REG Reference to a national code

Ref country code: IE

Ref legal event code: FG4D

Free format text: LANGUAGE OF EP DOCUMENT: GERMAN

REG Reference to a national code

Ref country code: DE

Ref legal event code: R096

Ref document number: 502013006711

Country of ref document: DE

REG Reference to a national code

Ref country code: NL

Ref legal event code: MP

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: FI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: NO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170622

Ref country code: LT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: GR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170623

REG Reference to a national code

Ref country code: LT

Ref legal event code: MG4D

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BG

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170622

Ref country code: RS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: SE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: LV

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: RO

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: SK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: CZ

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: EE

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IS

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170722

Ref country code: PL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: PT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170724

Ref country code: SM

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

REG Reference to a national code

Ref country code: DE

Ref legal event code: R097

Ref document number: 502013006711

Country of ref document: DE

PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DK

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

26N No opposition filed

Effective date: 20180102

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: SI

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

REG Reference to a national code

Ref country code: CH

Ref legal event code: PL

GBPC Gb: european patent ceased through non-payment of renewal fee

Effective date: 20180110

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MT

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: LU

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180110

Ref country code: FR

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180131

REG Reference to a national code

Ref country code: IE

Ref legal event code: MM4A

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

Effective date: 20180928

REG Reference to a national code

Ref country code: BE

Ref legal event code: MM

Effective date: 20180131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180110

Ref country code: BE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180131

Ref country code: LI

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180131

Ref country code: CH

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180131

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: IE

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180110

REG Reference to a national code

Ref country code: AT

Ref legal event code: MM01

Ref document number: 877769

Country of ref document: AT

Kind code of ref document: T

Effective date: 20180110

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20180110

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: MC

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: ES

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: TR

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: HU

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT; INVALID AB INITIO

Effective date: 20130110

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: CY

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

Ref country code: MK

Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES

Effective date: 20170322

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AL

Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT

Effective date: 20170322

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 20240129

Year of fee payment: 12