WO2013160292A1 - Procédé pour la séparation de mélanges comprenant des alcanes à chaîne droite et ramifiés par adsorption sur zif-77 - Google Patents

Procédé pour la séparation de mélanges comprenant des alcanes à chaîne droite et ramifiés par adsorption sur zif-77 Download PDF

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Publication number
WO2013160292A1
WO2013160292A1 PCT/EP2013/058376 EP2013058376W WO2013160292A1 WO 2013160292 A1 WO2013160292 A1 WO 2013160292A1 EP 2013058376 W EP2013058376 W EP 2013058376W WO 2013160292 A1 WO2013160292 A1 WO 2013160292A1
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alkane
molecular sieve
alkanes
branched
separating
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PCT/EP2013/058376
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English (en)
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David DUBBELDAM
Rajamani Krishna
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Universiteit Van Amsterdam
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Publication of WO2013160292A1 publication Critical patent/WO2013160292A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
    • C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/22—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material
    • B01J20/223—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising organic material containing metals, e.g. organo-metallic compounds, coordination complexes
    • B01J20/226—Coordination polymers, e.g. metal-organic frameworks [MOF], zeolitic imidazolate frameworks [ZIF]
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28054—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J20/28078—Pore diameter
    • B01J20/2808—Pore diameter being less than 2 nm, i.e. micropores or nanopores
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3433—Regenerating or reactivating of sorbents or filter aids other than those covered by B01J20/3408 - B01J20/3425
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/34—Regenerating or reactivating
    • B01J20/3491—Regenerating or reactivating by pressure treatment
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/02—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material
    • C10G25/03—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with ion-exchange material with crystalline alumino-silicates, e.g. molecular sieves
    • 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
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/12—Recovery of used adsorbent

Definitions

  • the present invention pertains to a process for separating a mixture of alkanes, which comprises straight-chain alkanes and branched alkanes into at least two fractions.
  • Mixtures of straight-chain and branched alkanes are formed in many hydrocarbon conversion processes, for example in oil refining, but also in other processes.
  • a case where the separation of alkanes with different degrees of branching is of particular importance is in the manufacture of gasoline.
  • the effluent of a paraffin isomerization reactor contains a mixture of normal alkanes, mono-methyl alkanes and di-methyl alkanes. Traditionally, only the normal alkanes are separated from the isomeric mixture by molecular sieving using LTA-type zeolite, and these linear alkanes are recycled to the
  • US4367364 describes a process for separating normal paraffins from cyclic and branched-chain hydrocarbons by contacting the mixture at adsorbent conditions with an adsorbent comprising silicalite.
  • the normal paraffin is adsorbed onto the silicalite .
  • the mono-methyl alkanes and di-methyl alkanes are collected for inclusion into the gasoline pool.
  • the di-methyl alkanes have the highest octane numbers and are the most desirable components. Therefore, a more efficient approach would be to separate only the di-methyl alkanes as product and recycle the normal and the mono-methyl alkanes to the isomerization reactor.
  • gasoline blending component by contacting a feed containing normal paraffins, mono-methyl-branched paraffins, and higher- branched paraffins with a separatory sieve which preferably is ferrierite.
  • the normal paraffins and mono-methyl-branched paraffins are adsorbed onto the separatory sieve, while the higher-branched paraffins are not.
  • the normal paraffins and mono-methyl-branched paraffins are desorbed from the molecular sieve, and recycled to the isomerisation unit.
  • isomerate gasoline blending component which uses a combination of two separatory sieves.
  • the first sieve which preferably is calcium 5A, selectively adsorbs the n-alkanes.
  • the second sieve selectively adsorbs the mono-methyl branched paraffins. The higher-branched isomers are not adsorbed.
  • a problem associated with the processes described above is that the separation process shows a relatively low selectivity for on the one hand, the straight chain and monomethyl alkanes with their relatively low octane numbers, and on the other hand the higher-branched alkanes with the more desirable octane numbers . There is therefore need for a process with a higher adsorption selectivity, allowing better separation between these groups of compounds. This allows on the one hand for better
  • the present invention provides such a process.
  • the present invention therefore pertains to a process for separating a mixture of alkanes which comprises straight-chain alkanes and branched alkanes, wherein the mixture is contacted with a molecular sieve under adsorption conditions resulting in adsorption of at least part of the alkane mixture onto the molecular sieve to form an adsorbed fraction, and subsequently subjecting the molecular sieve to desorption conditions thereby desorbing at least part of the adsorbed fraction from the molecular sieve, wherein the molecular sieve is a
  • Figure 1 shows the simulated adsorption selectivity as a function of the total pressure at 433 K (160°C) for various nanoporous materials.
  • Figure 2 shows the simulated pulse breakthrough curves of hexane isomers in ZIF-77 at 433 K (160°C) and 100 kPa total pressure .
  • Figure 3 shows the simulated pulse breakthrough curves of hexane isomers in MFI at 433 K (160°C) and 100 kPa total pressure .
  • Figure 4 shows the simulated pulse breakthrough curves of hexane isomers in CoBDP at 433 K (160°C) and 100 kPa total pressure.
  • Figure 5 shows the simulated pulse breakthrough curves of hexane isomers in MgMOF at 433 K (160°C) and 100 kPa total pressure .
  • Figure 6 shows the simulated pulse breakthrough curves of C5- C7 alkane isomers in ZIF-77 at 433 K (160°C) and 260 kPa total pressure .
  • Figure 7 shows a process overview of a C5/C6/C7 isomerisation / separation process using ZIF-77 in the separation step.
  • Figure 8 shows equimolar mixture adsorption isotherms at industrial conditions as a function of pressure for
  • Erionite is capable of separating only the linear alkane (n-hexane (C6) nC6) from the remainder (mono- and dibranched alkanes, 2- methylpentane (2MP) , 3-methylpentane (3MP) , 2 , 2-dimethylbutane (22DMB) , and 2 , 3-dimethylbutane (23DMB) .
  • Figure 8B shows that ZIF-77 is able to separate both linear and mono-branched alkanes from the di-branched molecules.
  • ERI- and LTA-type zeolites have 8-ring window and pore windows in the 4-5 Angstrom range.
  • the nanoporous material is therefore only accessible to linear alkanes due to size-exclusion.
  • Zeolites having a ZIF-77 topology allow also larger molecules in the structure, but shows a crucial order-of-magnitude difference in adsorption between linear, mono-branched, and dibranched molecules.
  • molecular sieves of ZIF-77 topology and pore size the ZIF-77 are able to separate both linear and mono-branched alkanes from the di-branched molecules. More generally, molecular sieves of ZIF-77 topology and pore size ZIF-77 are capable of separating linear from mono-branched from di-branched alkanes over a wide range of chain-lengths.
  • the temperature of 433 K is just for illustration; the
  • the adsorption selectivity of ZIF-77 has been found to be of the order of two factors, i.e. 100 times, higher than the adsorption selectivity of other molecular sieves.
  • This figure shows the simulated adsorption selectivity as a function of the total pressure at 433 K for various nanoporous materials.
  • ZIF- 77 has a significantly higher selectivity, as compared to other nanoporous materials (Note the log-scale on the y-axis) .
  • MFI of which family ZSM-5 and silicalite are members. However, MFI only shows a high selectivity at 100 bar. This means that for an MFI-containing system the high selectivity can only be obtained at pressures of 100 bar, while a molecular sieve of
  • ZIF-77 topology can be applied at much lower pressures, making for a process with increased economic performance.
  • ZIF-77 over MFI zeolite is that it allows fractionation of a mixture of C5, C6 and C7 isomers into individual components.
  • the dimethylisomers show a peak at a time range which is an order of magnitude smaller than the monomethyl isomers, which in turn show a peak at an order of magnitude smaller than the normal (straight chain) hexane.
  • the breakthrough of the dibranched molecules is first, followed by the
  • the diameter of the pores of the molecular sieve of this structure was found to be 3.6 A (R. Banerjee, A. Phan, B. Wang, C. Knobler, H. Furukawa, M. O'Keeffe, O.M. Yaghi, High-throughput
  • the molecular sieve with ZIF-77 topology preferably is ZIF-77 or a topological isomorph of ZIF-77.
  • ZIF-77 is used.
  • ZIF-77 is known in the art.
  • the structure (unit cell and atomic positions) of ZIF-77 is described in R. Banerjee,
  • ZIF-77 The manufacture of ZIF-77 is also known in the art. It is described, e.g., in WO2008/140788, in particular in [00207] and [00208] thereof. The synthesis of ZIF-77 is described in detail in the supplemental material of R. Banerjee, A. Phan,
  • Preferred topological isomorphs of ZIF-77 include structures having zeolite framework topologies in which all tetrahedral atoms are transition metals (denoted with 'M'), and all bridging ones are imidazolate (IM) units.
  • Preferred topological isomorphs of ZIF-77 comprise a
  • nitroimidazole linker wherein M is a transition metal, preferably selected from the group consisting of Fe(II), Co (II) and Cu(II) .
  • R is selected from the group consisting of Br, F, CI, NH2 and CH3.
  • the process according to the invention may be used for the separation of n-alkanes from branched alkanes.
  • the invention is particularly suitable for the separation of n-alkanes and monomethyl alkanes on the one hand and higher-branched, in particular dimethyl alkanes and higher-branched materials on the other hand.
  • the alkane may have 4-20 carbon atoms. In one embodiment, alkane has 4-12 carbon atoms, more in particular 4-8 carbon atoms, still more in particular 5-7 carbon atoms.
  • the process according to the invention is also suitable for separating mixtures containing n-alkanes of different chain lengths and their respective isomers.
  • the process according to the invention is used for separating a mixture comprising C4-C8 n-alkanes and their isomers, in particular monomethyl and dimethyl isomers.
  • the process is particularly suitable for separating a mixture comprising C5- C7 n-alkanes and their isomers, in particular monomethyl and dimethyl isomers. Separation of mixtures containing n-alkanes of different chain lengths and their respective isomers, which is of particular interest in the production of gasoline, will be discussed in more detail further on in this specification.
  • alkanes which comprises straight-chain alkanes and branched alkanes
  • a molecular sieve under adsorption conditions resulting in adsorption of at least part of the alkane mixture onto the molecular sieve to form an adsorbed fraction.
  • part of the mixture is adsorbed onto the molecular sieve to form an adsorbed fraction and part of the mixture is not adsorbed onto the molecular sieve.
  • the non-adsorbed fraction is separated from the molecular sieve.
  • Adsorption conditions are those conditions of temperature and pressure at which the fraction to be adsorbed is adsorbed onto the molecular sieve. Suitable conditions include an increased pressure, e.g., a pressure in the range of 1 bar to 1000 bar. It has been found that the high selectivity of ZIF-77 allows the use of lower pressures, which is highly attractive from a technical and economical point of view. Therefore, in one embodiment, the process is carried out at a pressure of 1-100 bar, more in particular at a pressure of 1-60 bar, still more in particular at a pressure if 1-40 bar.
  • the adsorption reaction can, e.g., take place at a temperature in the range of 370 to 550 K (97-277°C) .
  • Adsorption takes place in the gas phase. The same goes for the desorption step, which will be discussed in more detail below.
  • the molecular sieve is subjected to desorption conditions to remove at least part of the adsorbed fraction from the molecular sieve.
  • the desorption step can be carried out by means known in the art, e.g., by contacting the molecular sieve with a desorbent material at increased
  • Suitable desorbent materials may be gases such as gaseous hydrocarbons such as methane or ethane, or other gases, such as nitrogen on
  • Suitable desorbent materials may also be liquids, as long as they can be separated from the product fraction.
  • the crux of the desorption step is to purge at least part of the adsorbed fraction from the molecular sieve. It is within the scope of the skilled person to select a suitable desorbent material and accompanying desorbent conditions. In one
  • the desorption step is carried out by contacting the molecular sieve with a gas stream, in particular a stream comprising one or more of hydrogen, nitrogen, methane, or ethane.
  • a gas stream in particular a stream comprising one or more of hydrogen, nitrogen, methane, or ethane.
  • the temperature may, e.g., be in the range of 370 to 550K (97-277°C) .
  • the pressure may be in the range of, e.g., 1- 20 bar.
  • adsorption characteristics of molecular sieve of ZIF-77 typology are such that the energy of adsorption of different compounds is quite specific. This means that the use of a molecular sieve of ZIF-77 topology and pore size makes it possible to separate the di-methyl substituted compounds in great selectivity from the monosubstituted and straight-chain compounds .
  • the present invention therefore also pertains to a process wherein the step of subjecting the molecular sieve to desorption conditions is carried out in at least two steps, wherein in a first step the desorption conditions are such that a first part of the adsorbed fraction is desorbed from the molecular sieve, and in a second step the desorption conditions are such that a second part of the adsorbed
  • fraction is desorbed from the molecular sieve, with the chemical composition of the desorbed fraction being different. It is within the scope of the skilled person to determine on a case-by-case basis by routine trial and error which desorption conditions should be applied to desorb which fractions.
  • One parameter that is believed to be particularly suitable in this respect is the pressure. By applying a stepwise reduction in pressure the sequential desorption of different fractions can be achieved. It is also possible to separate an isomer mixture into different fractions by applying a sequence of adsorption- desorption steps.
  • contacting the feedstock with a molecular sieve of ZIF-77 topology can for example be carried out by feeding the feedstock to a reactor containing the molecular sieve in particulate form.
  • the molecular sieve may be employed, for example, in the form of a fixed bed, fluidized bed, or moving bed. As explained above, the molecular sieve may be subjected alternatingly to adsorbent and desorbent conditions. In the simplest embodiment of the invention the process setup
  • the process comprises a single reactor, which is alternatingly operated in adsorption and desorption mode.
  • the process is operated in a setup comprising at least two reactors comprising the molecular sieve, with the feed mixture being provided to a reactor that is operated under adsorption conditions, and a desorbent medium being provided to a reactor operated under desorbent conditions.
  • the configuration is a fixed bed of adsorbent.
  • the preferred mode of operation is continuous, wherein the bed is alternated between adsorbent and desorbent conditions.
  • this may be indicated as a "pressure-swing
  • the present invention finds application in the separation of numerous different alkane mixtures.
  • the invention provides the use of a molecular sieve as defined herein for separating a higher branched alkane and a lower branched alkane or for separating different dibranched alkanes from each other, in particular for separating 2 , 2-dibranched alkanes from other di-branched alkanes.
  • separating said a higher branched alkane and a lower branched alkane comprises
  • the invention is applied in a preferred embodiment.
  • the feedstock is a composition comprising at least 50 wt . % of alkanes with 4 to 8 carbon atoms, the composition comprising at least one of n-alkane and mono-methyl alkane with 4 to 8 carbon atoms, and dimethyl alkane with 4-8 carbon atoms.
  • the feedstock is contained with a molecular sieve of ZIF-77 topology under such conditions that the n-alkanes and the monomethylalkanes are adsorbed onto the molecular sieve, and the dimethylalkanes are not adsorbed. The dimethyl alkanes that are not adsorbed are separated from the molecular sieve.
  • the molecular sieve is subsequently subjected to desorption conditions to desorb at least part of the adsorbed fraction from the molecular sieve.
  • the feedstock is a composition comprising at least 50 wt . % of alkanes with 5 to 7 carbon atoms, the composition comprising at least one of n-alkane and mono-methyl alkane with 5 to 7 carbon atoms, and dimethyl alkane with 5-7 carbon atoms
  • a compound is adsorbed means that at least 80% of the compound as present in the starting mixture is adsorbed onto the molecular sieve, in particular at least 90 ⁇ 6 , more in
  • a compound is not adsorbed means that at most 20% of the compound as present in the starting mixture is adsorbed onto the molecular sieve, in particular at most 10%, more in particular at most 5%.
  • FIG. 6 shows the simulated pulse breakthrough curves of C5-C7 alkane isomers in ZIF-77 at 433 K (160°C) and 260 kPa total pressure. As can be seen from this figure, the
  • isomerisation unit where it is converted to higher-branched material .
  • the feedstock comprises at least 50 wt . % of alkanes with the stipulated number of carbon atoms, 4-8, in particular 5-7, preferably at least 70 wt.%, more preferably at least 80 wt.%. Other components may be present, as long as they do not interfere with the separation process. It is preferred for the feedstock to comprise at least 90 wt.% of alkanes with 4 to 8, in particular 5 to 7 carbon atoms, more preferably at least 95 wt.%. In one embodiment, the feedstock is derived from an isomerisation reactor.
  • the effluent desorbed from the molecular sieve which consists for at least 80 wt.% of n-alkanes and monomethyl alkanes is recycled back to the isomerisation unit.
  • Isomerisation processes are known in the art. Generally they comprise providing a feedstock to be isomerised to a reactor comprising an isomerisation catalyst under isomerisation conditions .
  • ZIF-77 is contacted with a feedstock containing a mixture of n-hexane, 2-methyl-pentane, 3-methyl pentane, 2,2-dimethyl butane, and 2,3-dimethyl butane.
  • the reaction conditions are a temperature of 433K (160°C) and an above-atmospheric pressure.
  • the feedstock is in the gas phase. After a certain time, the non-adsorbed fraction is removed from the feedstock. It will consist mainly of 2,2-dimethyl butane, and 2,3-dimethyl butane.
  • the molecular sieve is subjected to a desorption step by containing it with a desorbent material, e.g. a gas stream comprising one or more of hydrogen, nitrogen, methane, or ethane at a temperature in the range of 370 to 550K (97-277°C) and a pressure in the range of, e.g., 1-20 bar.
  • a mixture of C5-C7 alkanes is provided to an isomerisation reactor that comprises an isomerisation catalyst, e.g., a Group VIII noble metal on a mordenite.
  • the effluent from the isomerisation reactor which comprises n-alkanes, monomethyl- isomers, and dimethyl isomers, is provided to a reactor
  • a mixture of C5-C7 alkanes is provided to an isomerisation reactor that comprises an isomerisation catalyst, e.g., a Group VIII noble metal on a mordenite.
  • the effluent from the isomerisation reactor which comprises n-alkanes, monomethyl- isomers, and dimethyl isomers, is provided to a reactor
  • Erionite is capable of separating only the linear alkane (n-hexane (C6) nC6) from the remainder (mono- and dibranched alkanes, 2- methylpentane (2MP) , 3-methylpentane (3MP) , 2 , 2-dimethylbutane (22DMB) , and 2 , 3-dimethylbutane (23DMB) .
  • C6 linear alkane
  • 3MP 2-dimethylbutane
  • 23DMB 3-dimethylbutane

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Analytical Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
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  • Crystallography & Structural Chemistry (AREA)
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Abstract

L'invention porte sur un procédé pour la séparation d'un mélange d'alcanes qui comprend des alcanes à chaîne droite et des alcanes ramifiés, le mélange étant mis en contact avec un tamis moléculaire dans des conditions d'adsorption, ce qui a pour résultat l'adsorption d'au moins une partie du mélange d'alcanes sur le tamis moléculaire pour former une fraction adsorbée, et par la suite le tamis moléculaire étant soumis à des conditions de désorption pour de cette manière désorber du tamis moléculaire au moins une partie de la fraction adsorbée, le tamis moléculaire étant un tamis moléculaire ayant une topologie et une taille des pores de type ZIF-77. Il a été trouvé que l'utilisation d'un tamis moléculaire ayant une topologie et une taille des pores de type ZIF-77 a pour résultat un procédé ayant une sélectivité très élevée. Plus particulièrement, il a été trouvé qu'un matériau ayant cette structure présente une sélectivité d'adsorption élevée, définie comme la quantité adsorbée du total des alcanes à chaîne droite et des alcanes ramifiés monométhyliques divisée par la quantité adsorbée du total des alcanes ramifiés supérieurs. Une sélectivité d'adsorption élevée conduit à des plus petits volumes d'appareillage et de plus faibles besoins de capitaux et d'énergie.
PCT/EP2013/058376 2012-04-27 2013-04-23 Procédé pour la séparation de mélanges comprenant des alcanes à chaîne droite et ramifiés par adsorption sur zif-77 WO2013160292A1 (fr)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105032209A (zh) * 2015-07-10 2015-11-11 北京化工大学 一种用于气体分离的金属有机骨架zif-9膜的制备方法
WO2021032672A1 (fr) * 2019-08-16 2021-02-25 Global Bioenergies Alcanes ramifiés et leur procédé de préparation
WO2021190817A1 (fr) * 2020-03-27 2021-09-30 Global Bioenergies Oléfines et alcanes ramifiés et leur procédé de préparation

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US4717784A (en) 1986-12-10 1988-01-05 Shell Oil Company Total isomerization process with mono-methyl-branched plus normal paraffin recycle stream
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US6353144B1 (en) * 1998-02-04 2002-03-05 Institut Francais Du Petrole Process for chromatographic separation of a C5-C8 feed or an intermediate feed into three effluents, respectively rich in straight chain, mono-branched and multi-branched paraffins
WO2008140788A1 (fr) 2007-05-11 2008-11-20 The Regents Of The University Of California Séparation de gaz d'adsorption de gaz multi-composants

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US4367364A (en) 1981-07-30 1983-01-04 Uop Inc. Process for separating normal paraffins using silicalite adsorbent
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JP2022545206A (ja) * 2019-08-16 2022-10-26 ロレアル 分枝状アルカン及びこれを調製するための方法
WO2021190817A1 (fr) * 2020-03-27 2021-09-30 Global Bioenergies Oléfines et alcanes ramifiés et leur procédé de préparation

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