EP1154973A1 - Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4 - Google Patents

Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4

Info

Publication number
EP1154973A1
EP1154973A1 EP00915154A EP00915154A EP1154973A1 EP 1154973 A1 EP1154973 A1 EP 1154973A1 EP 00915154 A EP00915154 A EP 00915154A EP 00915154 A EP00915154 A EP 00915154A EP 1154973 A1 EP1154973 A1 EP 1154973A1
Authority
EP
European Patent Office
Prior art keywords
metal
process according
energy
hydrocarbons
methane
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.)
Withdrawn
Application number
EP00915154A
Other languages
German (de)
English (en)
Inventor
Michael Rennie Haines
Jeffrey Kwok-Sing Wan
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.)
Shell Internationale Research Maatschappij BV
Original Assignee
Shell Internationale Research Maatschappij BV
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 Shell Internationale Research Maatschappij BV filed Critical Shell Internationale Research Maatschappij BV
Priority to EP00915154A priority Critical patent/EP1154973A1/fr
Publication of EP1154973A1 publication Critical patent/EP1154973A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/76—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation of hydrocarbons with partial elimination of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/20—Vanadium, niobium or tantalum
    • C07C2523/22—Vanadium
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/24—Chromium, molybdenum or tungsten
    • C07C2523/30—Tungsten
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/16—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • C07C2523/32—Manganese, technetium or rhenium
    • C07C2523/34—Manganese
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper
    • C07C2523/72—Copper

Definitions

  • the present invention relates to a process for the production of aromatic hydrocarbons from a hydrocarbonaceous feedstock comprising C1--4 hydrocarbons.
  • the process especially comprises subjecting the hydro- carbonaceous feedstock to specific electromagnetic energy, especially microwave energy or radio frequency energy, in the presence of a catalyst comprising a metal and/or a metal oxide.
  • the types of catalysts that have been used for this and related processes include those based on metals or oxides of iron, cobalt, nickel and ruthenium, with and without promoters and/or supports.
  • the products obtained in the Fischer Tropsch reaction may be converted by other processes (hydrocracking, aromatization over zeolites etc.) into different products.
  • a potentially more useful and industrially applicable method for the direct conversion of methane into higher hydrocarbons is the use of high power pulsed energy, such as high power pulsed microwaves or high power pulsed radio frequency (Rf) energy.
  • high power pulsed energy such as high power pulsed microwaves or high power pulsed radio frequency (Rf) energy.
  • Rf radio frequency
  • Such processes are known in the literature. These conversions are highly energy activated processes and are based on similar mechanisms, differing in wavelengths generated and hardware required.
  • Rf operates in the 30-100 MHz range, microwave in the 1000-3000 MHz range, although in general all high power waves (especially between microwave and Rf) may be used.
  • These technologies generate electromagnetic waves which cause molecular excitation resulting in local temperature increase and/or the liberation and energisation of free electrons .
  • high temperature and elevated pressure are required to maintain the reaction on the catalytic surface.
  • Adsorbed reactants at such "hot” surface sites may acquire some of this energy and undergo reactions, otherwise the energy will then dissipate slowly into the matrix by conduction. Since only the surface is heated, there is a very large temperature gradient between the surface and the bulk of the gas phase, creating an efficient reactant circulation. Secondary reactions in the bulk will tend to be minimised by the much lower temperature of the gas phase. It has been shown that methane can be converted into mainly C2 and C3, using a reduced nickel catalyst. However, it will be appreciated that conversion of methane into higher hydrocarbons is an even more desired reaction.
  • C]__4 hydrocarbons can be directly converted in into aromatic hydrocarbons in a catalytic processes in which high power pulsed electromagnetic energy, e.g. microwave energy or radio frequency energy is used. It has been found that e.g. methane can be converted into especially benzene, toluene and xylene at high methane conversion levels and at high selectivities . Beside the aromatic hydrocarbons substantive amounts of hydrogen are formed. In particular, the process uses intense coherent microwave or radio frequency radiation applied in pulses to a metal sponge metal/metal oxide catalyst with a high voidage .
  • high power pulsed electromagnetic energy e.g. microwave energy or radio frequency energy
  • the present application relates to a process for the production of aromatic hydrocarbons from a hydrocarbonaceous feedstock comprising C]__4 hydro- carbons, comprising subjecting the hydrocarbonaceous feedstock to high power pulsed electromagnetic energy ranging from microwave energy to radio frequency energy in the presence of a catalyst comprising a metal and/or a metal oxide.
  • the feedstock to be used may be every feedstock comprising mainly, e.g. more than 95 vol.%, of C ⁇ _4 hydrocarbons of the total amount of hydrocarbons present .
  • Beside hydrocarbons other gasses may be present, e.g. nitrogen, carbon dioxide, noble gasses, or other gasses which are inert during the reaction.
  • at least 80 vol. percent of the hydrocarbons in the feedstock are methane and ethane, preferably at least 90 vol. percent of the hydrocarbons are methane.
  • Very suitably natural gas or associated gas may be used.
  • the metal or metal oxide used in the present invention is suitably derived from a transition metal.
  • Suitable transition metals or metal oxides are derived from a group I B, II B, V B, VI B, VII B or VIII metal, especially from a group I B, V B, VI B, VII B or VIII metal, more especially from a group I B, V B, VI B, or VII B metal.
  • the metal or metal oxide is derived from vanadium, tungsten, manganese, iron or copper, especially vanadium or tungsten. It will be appreciated that also mixtures can be used.
  • the metal or metal oxide can be used in many forms .
  • metal powders, metal foils, wires and gauzes may be used.
  • Also supported catalysts may be used.
  • the carrier is especially a metal structure, e.g. a woven metal wire structure, small mesh wire netting, gauze wire cloth, a metal fibre structure or a metal sponge, a carbon fibre structure, a mineral fibre structure or a refractory oxide structure, especially a metal sponge.
  • any metal or transition metal can be used, especially metal fibres having a diameter between .05 and 2.5 mm, especially between .1 and 1 mm, preferably between .2 and .5 mm.
  • transition metals especially copper or iron.
  • the above described carrier containing catalysts combine the desired properties of strong interaction with microwave energy by virtue of their metallic sites, with a means of dispersion the thermal energy to the supported material.
  • the large surface area of the porous catalyst facilitates the gaseous interaction and catalyses reactions further along the reaction sequence.
  • the carrier as such may also catalyse the reaction, although it is preferred to add an additional catalyst.
  • the term catalyst as used in connection with the present application also covers the bare metal carrier as defined above.
  • a suitable surface area of the carrier is between 10 and 100000 mm ⁇ /g, especially between 50 and 50000 mm ⁇ /g, more especially between 500 and 10000 mm ⁇ /g, preferably between 1000 and 5000 mm ⁇ /g.
  • the voidage of the catalyst is suitably at least 50 vol.%, especially at least 75 vol.%, suitably between 85 and 99.99 vol.%, especially between 90 and 99.9 vol. percent, preferably between 96 and 99.7 vol. percent.
  • the amount of hydrocarbon feedstock used per minute per amount of carrier used is suitably between .01 and 10 litre (273 K, 1 bar) of gaseous hydrocarbon feedstock per minute per gram of catalyst (carrier and catalyst when present) (but higher amounts, even up to 50 litres/g, are also possible), especially between 0.01 and 5 litre, preferably between 0.05 and 2 litre.
  • the amount of catalyst is preferably between 1 and 300 wt% percent of carrier, especially between 5 and 100 wt percent, preferably between 10 and 40 percent.
  • aromatic hydrocarbons prepared in the process according to the present invention are suitably benzene or mono- or di-alkylated benzene, especially benzene, toluene or xylene, but also ethyl benzene, diethyl benzene and t ⁇ metyl benzene.
  • the reaction according to the present invention may be carried out at all possible temperatures and pressures.
  • the temperature is suitably carried out between -20 and 250 °C, especially between 0 and 160 °C, preferably between 10 and 100 °C, especially at ambient temperature. It is observed that the above indicated temperatures relate to the incoming gas stream. Due to the processes involved, the temperature will increase during the reaction. Usually the processed gas stream will have a temperature which is up to 160 °C higher than the incoming gas stream, especially up to 80 °C higher. Further, it will be appreciated that much higher temperatures will exist at the surface of the catalyst.
  • the reaction is suitably carried out at a pressure between 0.2 and 30 bar, or even up to 50 bar or more, especially between 0.5 and 16 bar, preferably between .75 bar and 6 bar, especially at 1 to 2 bar. It is observed that during the reaction the pressure may increase due to an increase of the temperature and the formation of hydrogen .
  • the energy used in the process according to the present invention in a small scale experiment is suitably a continuous cycle of microwave power or radio frequency power between 200 and 1800 Watt, especially between 400 and 1400 Watt, preferably between 600 and 1000 Watt, for a period between .05 and 4 seconds, especially between .1 and 2 seconds, preferably between 0.4 and 1.0 seconds, followed by a period between 1 and 20 seconds, especially between 1.5 and 12 seconds, preferably between 2 and 8 seconds, without microwave power or radio frequency power.
  • the microwave power is emitted m the form of high energy pulses, suitably with a periodicity of between .5 and 70 milliseconds, especially between 3 and 40 milliseconds, preferably between 5 and 20 milliseconds.
  • the pulses suitably last for a period between .1 and 12 milliseconds, especially between .3 and 7, preferably between .5 and 3 milliseconds.
  • the pulse width as well as the amplitude may be increased.
  • the above mentioned energy amounts relate to power generated during the first period of the cycle, i.e. when the energy is emitted in the form of high energy pulses.
  • An attractive way to carry out the process according to the present invention is to use less energy after the first period of energy addition.
  • the second and following periods of energy supply may be carried out at a level of 15 to 80 percent of the level of the first period, especially at a level between 20 and 45 percent of the first pulse, preferably between 25 and 35 percent of the first pulse. In this way only a quarter to a third of the energy is required (when compared with the starting energy) .
  • the high energy used in the first period may be repeated after every 20 to 200 periods of energy supply, preferably after 30 to 100 periods a pulse train is used of about the same energy level as the first pulse.
  • the thermal efficiency of the process is usually above 40 percent, and is especially between 50 and 80 percent.
  • the amount of energy to be used in the process according to the present invention is suitably between 15 and 200 Watt for the conversion of 1 mol methane/hour, preferably between 20 and 60 Watt, more preferably between 30 and 45 Watt.
  • Watts per m 3 of the catalyst is suitably between 20 and
  • 4000 kW/m 3 preferably between 50 and 2400 kW/m 3 , more preferably between 100 and 1600 kW/mN it will be clear that these figures will be dependant on e.g. the particular catalyst and the density of the catalyst.
  • the amount of energy expressed in relation to the surface area of the carrier is suitably between 40 and 3200 kW/m 2 , especially between 80 and 1800 kW/m 2 , preferably between 120 and 1200 kW/m 2 .
  • the conversion of the hydrocarbonaceous feedstock comprising C]__4 hydrocarbons, especially the methane, is suitably at least 30 vol. percent, preferably between 50 and 99 percent, more preferably between 70 and
  • the selectivities to aromatic hydrocarbons obtained in the process according to the invention is usually more than 30, but is often between 50 and 85 wt% based on converted starting compound.
  • the aromatic compounds may be separated and worked up from the reaction mixture in the usual way.
  • a suitable method is cooling the reaction product to a temperature between 15 and 25 °C, followed by distillation.
  • Another way is to absorb the liquid hydrocarbons in a suitable liquid.
  • the hydrogen and gaseous hydrocarbons formed may be separated, and used for separate purposes.
  • the mixture may also be used for the generation of power, especially electricity, which can be used internally, e.g. for the generation of microwave or radio frequency power, or can be exported.
  • the aromatic compounds can be used as such, e.g. as solvents or as fuel, or converted into other valuable chemical compounds.
  • a preferred use of the hydrogen formed in the process of the present invention is the use as an additional hydrogen source in a Fischer Tropsch process.
  • the synthesis gas to be used in the Fischer Tropsch process may have a lower H2/CO ratio than the consumption ratio.
  • the H2/CO ratio is usually between 0.5 and 1.2, while in most Fischer Tropsch reaction, especially reactions using iron or cobalt catalysts, the consumption ratio is between 2.0 and 2.1.
  • Addition of the hydrogen produced in the process of this invention to coal- or heavy oil-derived synthesis gas may raise the H2/CO ratio to a ratio which is closer or equal to the consumption ratio.
  • methane or natural gas as feed for the synthesis gas preparation a very suitable process for the preparation of the synthesis gas is partial oxidation or catalytic partial oxidation. Such a process results in synthesis gas having an H2/CO ratio of 1.8-1.9.
  • the consumption ratio is usually 2.0 to 2.1.
  • the actual synthesis gas mixture which is contacted with the catalyst mixture may have a lower H2/CO ratio than the consumption ratio.
  • the use of a gas recycle may result in a lower H2/CO ratio.
  • the use of a two-stage Fischer Tropsch process with addition of hydrogen between the stages may result in a low H2/CO ratio for the first step.
  • the hydrogen produced in the present process may also be used in the synthesis of oxygenates, especially methanol and dimethylether, which oxygenates optionally may be converted into aliphatic hydrocarbons or aromatic hydrocarbons.
  • a preferred Fischer Tropsch process is a fixed or slurry bed process, using iron or cobalt based catalyst, preferably cobalt based catalysts. Especially cobalt on an alumina, silica or titania carrier is used, optionally promoted by rhenium, platinum, manganese, zirconium or scandium.
  • the excess hydrogen produced in the present process may also be used for the upgrading of the hydrocarbons made in the Fischer Tropsch process. It may be used in any hydrocracking process, hydrogenation process or hydrotreatment process (e.g. hydrofinishing). It may also be used for the purification (e.g. desulphurization) of hydrocarbonaceous feed used for the preparation of the synthesis gas. Examples
  • a pulse controller was connected to the power supply to control the pulse period and the duty cycles that were simultaneously monitored by a digital oscilloscope.
  • the quartz tube chemical reactor (25 cm long and 1.7 cm in diameter) housed in the waveguide cavity was placed perpendicular to the direction of the microwave propagation and to the electric field so as to maximise the exposure to the incident microwave irradiation.
  • Controlled microwave experiments were performed in a batch reactor system in which the reactant gas was circulated through the catalytic bed with a peristaltic pump.
  • a dry-ice condenser was connected downstream of a GC sampling valve to trap liquid product.
  • Fe sponge based catalysts were prepared by physical mixing of Fe sponge with commercial; or custom made metal or metal oxide powders. The weight ratio of Fe sponge to metal powder was about 0.3 to 1.
  • Activated carbon and silica supported metal catalysts were prepared by impregnation methods, and then subjected to H2 reduction at 773 K for 2 h. The loading amount was 10 wt%.
  • Cu wire and Cu net catalysts were also used for comparison.
  • the typical reaction conditions were: pure CH4 at atmospheric pressure, flow rate 40 ml/mm, 0.25 g catalyst, incident microwave power 800 W, total irradiation time 1.8 s (15 pulses, 35 s rest time) . Optimum reaction conditions were achieved by varying the incident microwave power, the reaction pressure and the pulse sequence.
  • Porapak-Q packed column The selectivity to aromatics was calculated based on C-containmg products, which represents the fraction of methane that was converted to specific hydrocarbon products taking into account the number of carbon atoms m the molecule.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

L'invention concerne un procédé relatif à l'élaboration d'hydrocarbures aromatiques à partir d'une charge hydrocarburée comprenant des hydrocarbures C1-4. Le procédé consiste en particulier à soumettre la charge à une énergie électromagnétique spécifique, notamment l'énergie micro-onde ou l'énergie radioélectrique, en présence d'un catalyseur comprenant un métal et/ou un oxyde métallique. Il apparaît que le méthane peut être converti spécialement en benzène, en toluène et en xylène, avec des niveaux élevés de conversion de méthane et de sélectivité.
EP00915154A 1999-02-26 2000-02-25 Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4 Withdrawn EP1154973A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP00915154A EP1154973A1 (fr) 1999-02-26 2000-02-25 Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
EP99301485 1999-02-26
EP99301485 1999-02-26
EP00915154A EP1154973A1 (fr) 1999-02-26 2000-02-25 Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4
PCT/EP2000/001644 WO2000050366A1 (fr) 1999-02-26 2000-02-25 Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c¿1-4?

Publications (1)

Publication Number Publication Date
EP1154973A1 true EP1154973A1 (fr) 2001-11-21

Family

ID=8241246

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00915154A Withdrawn EP1154973A1 (fr) 1999-02-26 2000-02-25 Procede relatif a l'elaboration d'hydrocarbures aromatiques a partir d'hydrocarbures c1-4

Country Status (8)

Country Link
EP (1) EP1154973A1 (fr)
JP (1) JP2002537365A (fr)
AU (1) AU3656500A (fr)
BR (1) BR0008546A (fr)
CA (1) CA2364261A1 (fr)
EA (1) EA200100915A1 (fr)
NO (1) NO20014118L (fr)
WO (1) WO2000050366A1 (fr)

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
MY139252A (en) * 2004-10-04 2009-09-30 Shell Int Research Catalyst structure
JP5255845B2 (ja) * 2004-12-22 2013-08-07 エクソンモービル・ケミカル・パテンツ・インク メタンからのアルキル化芳香族炭化水素の製造
JP4905849B2 (ja) * 2006-04-07 2012-03-28 東京電力株式会社 マイクロ波を用いたジメチルエーテルの合成方法
CN101506129B (zh) * 2006-05-31 2014-01-01 埃克森美孚化学专利公司 同位素分析用于测定由甲烷制备的芳族烃的用途
WO2009091336A1 (fr) * 2008-01-16 2009-07-23 Agency For Science, Technology And Research Préparation de catalyseurs et méthodes d'utilisation de ceux-ci
WO2011058619A1 (fr) * 2009-11-10 2011-05-19 進藤 隆彦 Procédé de production d'un hydrocarbure saturé linéaire selon un procédé gtl direct gtl
US8609917B2 (en) 2010-01-19 2013-12-17 Uop Llc Process for increasing methyl to phenyl mole ratios and reducing benzene content in a motor fuel product
US8598395B2 (en) 2010-01-19 2013-12-03 Uop Llc Process for increasing a mole ratio of methyl to phenyl
US8563795B2 (en) 2010-01-19 2013-10-22 Uop Llc Aromatic aklylating agent and an aromatic production apparatus
CN103769191B (zh) * 2014-01-08 2016-08-17 华东理工大学 用于f-t合成蜡油轻度加氢裂解的催化剂、反应装置及反应方法
US10889763B2 (en) * 2018-03-16 2021-01-12 West Virginia University Methods and compositions for microwave-assisted non-oxidative catalytic direct conversion of natural gas

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR690028A (fr) * 1929-02-16 1930-09-15 Ruhrchemie Ag Procédé combiné permettant d'obtenir des hydrocarbures supérieurs
US2139969A (en) * 1937-02-12 1938-12-13 Eugene C Mills Process for converting gaseous hydrocarbons into liquid hydrocarbons

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO0050366A1 *

Also Published As

Publication number Publication date
WO2000050366A1 (fr) 2000-08-31
NO20014118L (no) 2001-10-12
NO20014118D0 (no) 2001-08-24
CA2364261A1 (fr) 2000-08-31
JP2002537365A (ja) 2002-11-05
BR0008546A (pt) 2001-11-06
EA200100915A1 (ru) 2002-02-28
AU3656500A (en) 2000-09-14

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