EP2802637B1 - 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 Download PDF

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Publication number
EP2802637B1
EP2802637B1 EP13700159.0A EP13700159A EP2802637B1 EP 2802637 B1 EP2802637 B1 EP 2802637B1 EP 13700159 A EP13700159 A EP 13700159A EP 2802637 B1 EP2802637 B1 EP 2802637B1
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Prior art keywords
cut
crude
hydrocarbons
vaporous
purified
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German (de)
English (en)
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EP2802637A1 (fr
Inventor
Bernd Heida
Randolf Hugo
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BASF SE
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BASF SE
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    • 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 process for providing a gaseous purified crude C 4 cut as feed stream for 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.
  • C 4 cuts are obtained in the catalytic dehydrogenation of n-butane and / or n-butene.
  • C 4 cuts usually 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.
  • 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 cuts 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 feed of the crude C 4 cut for extractive distillation in order to obtain a reliable Ensure operation of the extractive distillation.
  • Impurities leading to the above problems are especially higher than 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.
  • 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% by weight, based on the total weight of the crude C 4 cut
  • 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; this is 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 depleted with C 3 components crude C 4 stream is almost completely evaporated, and indeed flow controlled, so that the high-boiling compared to 1,3-butadiene components in the remaining liquid content not more than 5 wt .-%, in particular not above 1 wt .-%, or even not more than 0.1 wt .-%, based on the total weight of the evaporator vessel supplied raw C 4 cut 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.
  • the US 4,419,188 A describes a process for extractive distillation in a plurality of distillation columns wherein a plurality of thermally coupled extractive distillation steps are carried out.
  • This object is achieved by a process for providing a gaseous purified crude C 4 fraction as feed stream for an extractive distillation with a selective solvent,
  • 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.
  • a typical crude C 4 cut from a naphtha cracker has the following composition in weight percent: propane 0 - 0.5 propene 0 - 0.5 propadiene 0 - 0.5 propyne 0 - 0.5 n-butane 3 - 10 i-butane 1 - 3 1-butene 10 - 20 i-butene 10 - 30 trans-2-butene 2 - 8 cis-2-butene 2 - 6 1,3-butadiene 35 - 65 1,2-butadiene 0.1 -1 ethyl acetylene 0.1 - 2 vinyl acetylene 0.1 - 3 C5 0 - 0.5
  • 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.
  • extractive distillation are as selective solvents generally substances or mixtures in question, 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, more preferably dipolaraprotician solvent. 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 cyclic 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, dieth
  • N-alkyl substituted lower aliphatic acid amides or N-alkyl substituted cyclic acid amides are used. Particularly advantageous are dimethylformamide, acetonitrile, furfurol and in particular N-methylpyrrolidone.
  • mixtures of these solvents with one another for example of 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.
  • 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 crude C 4 cut , or more preferably less than 4 wt. ppm, depleted in a distillation column upstream of the evaporator boiler.
  • the C 5+ hydrocarbons are more preferably in the vapor purified crude C 4 fraction is depleted to less than half of the C 5+ hydrocarbons contained 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.
  • 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 fed 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 another preferred embodiment in which the evaporator boiler 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 % iso-butane, 19.0% n-butene, 28.3% iso-butene, 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 bottom stream is fed to an evaporator vessel for the purpose of separating off the components boiling high in relation to 1,3-butadiene, ie an apparatus with a single separation stage.
  • 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 do not exceed 5% by weight in the remaining liquid fraction.
  • Based on the total weight supplied to the evaporator vessel raw C 4 cut 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 may come into consideration, which are not taken into consideration here
  • 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.

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  • 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)

Claims (9)

  1. Procédé pour réaliser une distillation extractive à l'aide d'un solvant sélectif, pour produire du 1,3-butadiène brut, avec une fraction (2) brute, purifiée, sous forme vapeur, en C4 comme flux de départ, la fraction brute, purifiée, sous forme vapeur, en C4 étant obtenue, partant d'une fraction (1) brute liquide en C4 comme flux d'alimentation, contenant, outre des butanes, des butènes et du 1,3-butadiène, des hydrocarbures en C3, des oligomères et des polymères en C4 ainsi que des hydrocarbures en C5+, dans un procédé présentant les étapes de procédé
    1) séparation des oligomères et des polymères en C4 ainsi que des hydrocarbures en C5+, à chaque fois jusqu'aux teneurs résiduelles indiquées précédemment pour la fraction brute, purifiée, sous forme vapeur, en C4 et
    2) évaporation de la fraction liquide brute en C4 dans une cuve d'évaporation (VK),
    et la fraction brute, purifiée, sous forme vapeur en C4 contenant
    - moins de deux tiers des hydrocarbures en C5+ contenus dans le flux d'alimentation et
    - moins de 5% en poids des oligomères et polymères
    en C4 contenus dans le flux d'alimentation, caractérisé en ce qu'une colonne d'épuisement (K), présentant un ou plusieurs étages de séparation, dans laquelle est introduite la fraction (1) liquide en C4 dans la partie supérieure, qui est en échange direct gazeux et liquide, dans la partie inférieure, avec la cuve d'évaporation (VK) et à partir de laquelle, dans la partie supérieure, on soutire la fraction (2) brute en C4 purifiée sous forme de vapeur, est associée à la cuve d'évaporation (VK), la colonne d'épuisement (K) étant exploitée sans condensateur en tête de colonne.
  2. Procédé selon la revendication 1, caractérisé en ce que la colonne d'épuisement (K) est placée sur la cuve d'évaporation.
  3. Procédé selon la revendication 1, caractérisé en ce que la colonne d'épuisement (K) est adjointe à la cuve d'évaporation (VK) sous forme d'appareil séparé.
  4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que les hydrocarbures en C3 dans la fraction brute, purifiée, sous forme vapeur, en C4, sont épuisés jusqu'à moins de 10 ppm en poids par rapport au poids total de la fraction brute, purifiée, sous forme vapeur, en C4 dans une colonne de distillation disposée en amont de la cuve d'évaporation (VK).
  5. Procédé selon la revendication 4, caractérisé en ce que les hydrocarbures en C3 dans la fraction brute, purifiée, sous forme vapeur, en C4, sont épuisés jusqu'à moins de 4 ppm en poids par rapport au poids total de la fraction brute, purifiée, sous forme vapeur, en C4.
  6. Procédé selon l'une quelconque des revendications 1 à 5, caractérisé en ce que les hydrocarbures en C5+ dans la fraction brute, purifiée, sous forme vapeur, en C4 sont épuisés à moins de la moitié des hydrocarbures en C5+ contenus dans le flux d'alimentation.
  7. Procédé selon l'une quelconque des revendications 1 à 6, caractérisé en ce que la colonne d'épuisement (K) est exploitée à une pression de tête dans la plage de 3 à 7 bars absolus.
  8. Procédé selon la revendication 7, caractérisé en ce que la colonne d'épuisement (K) est exploitée à une pression de tête dans la plage de 4,5 à 5,5 bars absolus.
  9. Procédé selon l'une quelconque des revendications 1 à 8, caractérisé en ce que la colonne d'épuisement (K) présente 1 à 15 plateaux théoriques.
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 EP2802637A1 (fr) 2014-11-19
EP2802637B1 true EP2802637B1 (fr) 2017-03-22

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

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CN112135809A (zh) * 2018-05-18 2020-12-25 沙特基础工业全球技术有限公司 利用水合单元生产燃料添加剂的方法

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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
EP1766310A4 (fr) * 2004-07-06 2011-12-28 Fluor Tech Corp Configurations et procédés de séparation de condensats gazeux à partir de mélanges d"hydrocarbures à haute pression
EP2043977B1 (fr) * 2006-07-12 2012-10-10 Basf Se Procede de separation d'une fraction en c4 par distillation extractive avec un solvant selectif
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

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JP2015508409A (ja) 2015-03-19
CN104053752A (zh) 2014-09-17
JP6067748B2 (ja) 2017-01-25
KR102049312B1 (ko) 2019-11-28
WO2013104692A1 (fr) 2013-07-18
EP2802637A1 (fr) 2014-11-19
KR20140120329A (ko) 2014-10-13
CN104053752B (zh) 2016-08-31

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