US20150018592A1 - Direct synthesis of dme at equilibrium - Google Patents

Direct synthesis of dme at equilibrium Download PDF

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Publication number
US20150018592A1
US20150018592A1 US14/375,256 US201314375256A US2015018592A1 US 20150018592 A1 US20150018592 A1 US 20150018592A1 US 201314375256 A US201314375256 A US 201314375256A US 2015018592 A1 US2015018592 A1 US 2015018592A1
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US
United States
Prior art keywords
dme
syngas
product stream
process according
direct synthesis
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.)
Abandoned
Application number
US14/375,256
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English (en)
Inventor
Nicole Schodel
Ernst Haidegger
Holger Schmigalle
Volker Goke
Christian Thaller
Harald Schmaderer
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Linde GmbH
Original Assignee
Linde GmbH
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
Priority claimed from DE102012001811A external-priority patent/DE102012001811A1/de
Priority claimed from DE201210001803 external-priority patent/DE102012001803A1/de
Application filed by Linde GmbH filed Critical Linde GmbH
Assigned to LINDE AKTIENGESELLSCHAFT reassignment LINDE AKTIENGESELLSCHAFT ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SCHMIGALLE, NAREE, GOKE, VOLKER, HAIDEGGER, ERNST, SCHMADERER, Harald, SCHODEL, NICOLE, THALLER, CHRISTIAN
Publication of US20150018592A1 publication Critical patent/US20150018592A1/en
Abandoned legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
    • C07C41/01—Preparation of ethers
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • C07C1/22—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms by reduction
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0238—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a carbon dioxide reforming step
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the invention relates to a process for production of DME (dimethyl ether) as classified in the preamble of claim 1 .
  • a process of this type includes at least the steps of: generating a syngas containing CO and H 2 in a device for syngas generation (e.g. in a syngas reactor), such a device being any device suitable for syngas generation, and passing the syngas into a DME reactor for direct synthesis of DME by catalysed conversion of the syngas by means of a catalyst to form a product stream (reactor effluent) containing DME, CO 2 , H 2 O, CH 3 OH and unconverted syngas (CO and H 2 ).
  • a device for syngas generation e.g. in a syngas reactor
  • a device for syngas generation e.g. in a syngas reactor
  • the syngas mixture of CO and H 2 can be produced from natural gas, for example by steam reforming:
  • Syngas can further also be generated through what is known as autothermal reforming (combination of steam reforming and partial oxidation in one apparatus).
  • autothermal reforming combination of steam reforming and partial oxidation in one apparatus.
  • the two processes are combined with each other such that the advantage of the oxidation (provision of thermal energy) and the advantage of steam reforming (higher yield of hydrogen) complement each other to advantage.
  • syngas is also obtainable through what is known as combined reforming (combination of steam reforming and partial oxidation in separate apparatuses).
  • the DME reactor effluent also includes a large amount of unconverted syngas owing to the typically low rate of conversion. Gas separation is accordingly costly and inconvenient, since unconverted syngas is to be recycled into the DME reactor, whereas the CO 2 formed has to be recycled into the syngas part (syngas generation) in the natural gas-based embodiment of the process described at the beginning.
  • the problem addressed by the present invention is therefore that of providing a process that permits a comparatively simple gas separation.
  • This process provides that the direct synthesis is carried out at or close to the chemical equilibrium in order that the concentration of syngas in the said product stream may be reduced distinctly. It is preferable to use for this purpose a Cu-based catalyst which has an acidic functionality for a corresponding high activity and selectivity for DME (bifunctional catalyst). The functionality referred to favours in particular the elimination of water as per 2CH 3 OH—>DME+H 2 O.
  • the equilibrium concentration of dimethyl ether is present when the reaction of carbon monoxide and hydrogen to form dimethyl ether and carbon dioxide is in chemical equilibrium.
  • the chemical equilibrium of the reaction is reached when the rate of the forward reaction (3H 2 +3CO ⁇ DME+CO 2 ) is equal to the rate of the reverse reaction (DME+CO 2 ⁇ 3H 2 +3CO).
  • the direct synthesis in the DME reactor is at least carried out until achievement of a DME concentration in the reactor effluent amounting to at least 70%, at least 80%, at least 85% or at least 90% of the chemical equilibrium concentration of DME.
  • the DME reactor product stream containing CO, H 2 , CO 2 , DME, H 2 O and methanol is cooled to separate the remaining (in particular low-concentrated) syngas and also CO2 from a DME-rich (liquid) phase, so CO2, H2 and CO can be withdrawn for example overhead from a column as gaseous phase and DME can be withdrawn as bottom product in a liquid phase.
  • the gaseous phase is then preferably recycled into the syngas part (syngas generation).
  • DME repellent, solvent, LPG admixture, power fuel, feedstuff for olefin synthesis, . . .
  • further separation steps may optionally be carried out to remove CO 2 , methanol or water from the said liquid phase.
  • a further aspect of the present invention is a process for production of DME comprising the steps of:
  • the syngas to be introduced into the DME reactor is produced by dry reforming wherein methane and carbon dioxide are converted into carbon monoxide and hydrogen.
  • This dry reforming is advantageously carried out in the presence of a modified, soot-resistant nickel-based catalyst of the type also used in similar fashion in steam-reforming processes.
  • the dry-reforming process is advantageously carried out at a temperature between 750° C. and 950° C.
  • Methane for the purposes of the invention also comprehends methane-containing gases such as natural gas.
  • Dry reforming for the purposes of the invention is to be understood as meaning the conversion of methane or natural gas and CO 2 by heating in the absence of water into a syngas having a stoichiometric ratio of about 1:1 for H 2 and CO. Dry reforming for the purposes of the invention more particularly also comprehends the conversion of CH 4 or natural gas and CO 2 in the presence of water vapour, although water is only present in a stoichiometric ratio of 1:2, 1:3, 1:4, 1:5, 1:10 or 1:20 in relation to methane or natural gas.
  • dry reforming for the purposes of this invention more particularly requires the molar ratio of water to carbon in the feed to be less than 2:1 and preferably less than 1:1.
  • DME can further be converted in an olefin synthesis step into a product comprising olefins, especially ethylene and/or propylene, in which case the product stream is fed directly to the olefin synthesis step.
  • a product comprising olefins, especially ethylene and/or propylene
  • CO 2 can be separated from the product stream and then the product stream be fed to the olefin synthesis step.
  • the pressure difference between the direct synthesis in the DME reactor and the generation of syngas is not more than 3 bar and preferably not more than 1 bar at the point of exit from the syngas generation and at the point of entry into the DME reactor.
  • FIG. 1 shows a block diagram of a process according to the invention.
  • FIG. 1 shows a block diagram of an inventive process for production of DME by direct synthesis from syngas (CO and H 2 ).
  • Syngas is generated in a syngas step (syngas generation) 11 from natural gas 10 , for example by steam reforming.
  • the syngas 12 is passed into a DME reactor and reacted in the presence of an appropriately designed Cu-based catalyst (see above) into DME while the reactor is operated at or close to the chemical equilibrium:
  • the reactor effluent stream (product stream) 14 containing CO, H2, CO2, DME, H2O and methanol is fed from the DME reactor 13 into a separation step 15 in which the reactor effluent is cooled to obtain a gaseous phase containing CO, H2 and CO2, which is recycled into the synthesis part 14 , and a liquid phase 17 , which is a DME-enriched state.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Hydrogen, Water And Hydrids (AREA)
US14/375,256 2012-01-31 2013-01-15 Direct synthesis of dme at equilibrium Abandoned US20150018592A1 (en)

Applications Claiming Priority (7)

Application Number Priority Date Filing Date Title
DE102012001811A DE102012001811A1 (de) 2012-01-31 2012-01-31 Direktsynthese von DME am Gleichgewicht
DE201210001803 DE102012001803A1 (de) 2012-01-31 2012-01-31 Verfahren zur Herstellung von Dimethylether aus Methan
DE102012001803.7 2012-01-31
DE102012001811.8 2012-01-31
EP12001135.8 2012-02-21
EP12001135 2012-02-21
PCT/EP2013/000101 WO2013113467A1 (de) 2012-01-31 2013-01-15 Direktsynthese von dme am gleichgewicht

Publications (1)

Publication Number Publication Date
US20150018592A1 true US20150018592A1 (en) 2015-01-15

Family

ID=47559453

Family Applications (2)

Application Number Title Priority Date Filing Date
US14/375,891 Expired - Fee Related US9090543B2 (en) 2012-01-31 2013-01-15 Method for producing dimethyl ether from methane
US14/375,256 Abandoned US20150018592A1 (en) 2012-01-31 2013-01-15 Direct synthesis of dme at equilibrium

Family Applications Before (1)

Application Number Title Priority Date Filing Date
US14/375,891 Expired - Fee Related US9090543B2 (en) 2012-01-31 2013-01-15 Method for producing dimethyl ether from methane

Country Status (9)

Country Link
US (2) US9090543B2 (de)
EP (2) EP2809639B1 (de)
CN (1) CN104159880A (de)
BR (1) BR112014018062A8 (de)
CA (2) CA2860874A1 (de)
ES (2) ES2565668T3 (de)
RU (1) RU2014135473A (de)
WO (2) WO2013113467A1 (de)
ZA (2) ZA201405279B (de)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160130204A1 (en) * 2014-11-12 2016-05-12 Andreas Peschel Process and plant for preparation of one or more reaction products
WO2017176422A1 (en) * 2016-04-04 2017-10-12 Exxonmobil Research And Engineering Company Systems and methods for producing dimethyl ether from natural gas
US9938217B2 (en) 2016-07-01 2018-04-10 Res Usa, Llc Fluidized bed membrane reactor
US9981896B2 (en) 2016-07-01 2018-05-29 Res Usa, Llc Conversion of methane to dimethyl ether
US10189763B2 (en) 2016-07-01 2019-01-29 Res Usa, Llc Reduction of greenhouse gas emission
US20190111836A1 (en) * 2017-10-16 2019-04-18 Jvis-Usa, Llc Illuminated vehicle interior assembly such as a safety belt buckle assembly
EP3872029A1 (de) 2020-02-29 2021-09-01 Linde GmbH Verfahren und anlage zur herstellung eines syntheseprodukts

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EP3303217B1 (de) * 2015-05-29 2023-01-25 Szego, Eduardo Luigi Verfahren zur synthese einer reduzierenden gasmischung aus einem kohlenwasserstoffstrom und kohlendioxid
GB2551314B (en) 2016-06-06 2021-03-17 Kew Tech Limited Equilibium approach reactor
CN106701229A (zh) * 2016-12-30 2017-05-24 李卫教 一种二氧化碳与甲醇转化天然气的装置
WO2020150067A1 (en) 2019-01-18 2020-07-23 Exxonmobil Research And Engineering Company Layered catalyst loading for synthesis gas conversion
US11384289B2 (en) 2019-01-18 2022-07-12 ExxonMobil Technology and Engineering Company Conversion of methanol to gasoline with integrated paraffin conversion
US11426708B2 (en) 2020-03-02 2022-08-30 King Abdullah University Of Science And Technology Potassium-promoted red mud as a catalyst for forming hydrocarbons from carbon dioxide
US11420915B2 (en) 2020-06-11 2022-08-23 Saudi Arabian Oil Company Red mud as a catalyst for the isomerization of olefins
US11495814B2 (en) 2020-06-17 2022-11-08 Saudi Arabian Oil Company Utilizing black powder for electrolytes for flow batteries
US11814289B2 (en) 2021-01-04 2023-11-14 Saudi Arabian Oil Company Black powder catalyst for hydrogen production via steam reforming
US11427519B2 (en) 2021-01-04 2022-08-30 Saudi Arabian Oil Company Acid modified red mud as a catalyst for olefin isomerization
US11820658B2 (en) 2021-01-04 2023-11-21 Saudi Arabian Oil Company Black powder catalyst for hydrogen production via autothermal reforming
US11724943B2 (en) 2021-01-04 2023-08-15 Saudi Arabian Oil Company Black powder catalyst for hydrogen production via dry reforming
US11718522B2 (en) 2021-01-04 2023-08-08 Saudi Arabian Oil Company Black powder catalyst for hydrogen production via bi-reforming
US11787759B2 (en) 2021-08-12 2023-10-17 Saudi Arabian Oil Company Dimethyl ether production via dry reforming and dimethyl ether synthesis in a vessel
US11578016B1 (en) 2021-08-12 2023-02-14 Saudi Arabian Oil Company Olefin production via dry reforming and olefin synthesis in a vessel
US11718575B2 (en) 2021-08-12 2023-08-08 Saudi Arabian Oil Company Methanol production via dry reforming and methanol synthesis in a vessel
US11617981B1 (en) 2022-01-03 2023-04-04 Saudi Arabian Oil Company Method for capturing CO2 with assisted vapor compression

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6852897B2 (en) * 2000-06-23 2005-02-08 Jgc Corporation Process for the preparation of lower olefins

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2097382B (en) * 1981-04-28 1984-11-14 Mobil Oil Corp Conversion of syngas into dimethyl ether
DK171707B1 (da) * 1995-02-03 1997-04-01 Topsoe Haldor As Fremgangsmåde til fremstilling af dimetylæter i brændstofkvalitet
JP4189068B2 (ja) 1998-09-30 2008-12-03 千代田化工建設株式会社 低級炭化水素ガスからジメチルエーテルを製造する方法
CA2604574C (en) * 2005-04-15 2013-11-19 University Of Southern California Selective oxidative conversion of methane to methanol, dimethyl ether and derived products
KR100732784B1 (ko) * 2005-06-17 2007-06-27 한국가스공사 탄화수소로부터 디메틸에테르를 제조하는 방법
US7906559B2 (en) 2007-06-21 2011-03-15 University Of Southern California Conversion of carbon dioxide to methanol and/or dimethyl ether using bi-reforming of methane or natural gas
EP2119668A3 (de) * 2008-05-16 2012-04-18 Haldor Topsoe A/S Verfahren zur Herstellung von Synthesegas aus Schwarzlauge

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6852897B2 (en) * 2000-06-23 2005-02-08 Jgc Corporation Process for the preparation of lower olefins

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Moradi et al. "Equilibrium Calculations for Direct Synthesis of Dimethy Ether from Syngas." The Canadian Journal of Chemical Engineering. Volume 89 February 2011, pages 108-115. *

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160130204A1 (en) * 2014-11-12 2016-05-12 Andreas Peschel Process and plant for preparation of one or more reaction products
US9718751B2 (en) * 2014-11-12 2017-08-01 Linde Aktiengesellschaft Process and plant for preparation of one or more reaction products
WO2017176422A1 (en) * 2016-04-04 2017-10-12 Exxonmobil Research And Engineering Company Systems and methods for producing dimethyl ether from natural gas
US10160708B2 (en) 2016-04-04 2018-12-25 Exxonmobil Research And Engineering Company Systems and methods for producing dimethyl ether from natural gas
US9938217B2 (en) 2016-07-01 2018-04-10 Res Usa, Llc Fluidized bed membrane reactor
US9981896B2 (en) 2016-07-01 2018-05-29 Res Usa, Llc Conversion of methane to dimethyl ether
US10189763B2 (en) 2016-07-01 2019-01-29 Res Usa, Llc Reduction of greenhouse gas emission
US20190111836A1 (en) * 2017-10-16 2019-04-18 Jvis-Usa, Llc Illuminated vehicle interior assembly such as a safety belt buckle assembly
EP3872029A1 (de) 2020-02-29 2021-09-01 Linde GmbH Verfahren und anlage zur herstellung eines syntheseprodukts

Also Published As

Publication number Publication date
WO2013113467A1 (de) 2013-08-08
BR112014018062A2 (de) 2017-06-20
US20150045456A1 (en) 2015-02-12
ES2565667T3 (es) 2016-04-06
BR112014018062A8 (pt) 2017-07-11
CA2860876A1 (en) 2013-08-08
EP2809640A1 (de) 2014-12-10
EP2809639A1 (de) 2014-12-10
US9090543B2 (en) 2015-07-28
ZA201405279B (en) 2016-01-27
WO2013113468A1 (de) 2013-08-08
CA2860874A1 (en) 2013-08-08
RU2014135473A (ru) 2016-03-20
ES2565668T3 (es) 2016-04-06
EP2809639B1 (de) 2016-01-13
ZA201405278B (en) 2016-11-30
CN104159880A (zh) 2014-11-19
EP2809640B1 (de) 2016-01-13

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