[go: up one dir, main page]

US20130046033A1 - Process for the Production of Light Olefins from Synthesis Gas - Google Patents

Process for the Production of Light Olefins from Synthesis Gas Download PDF

Info

Publication number
US20130046033A1
US20130046033A1 US13/695,743 US201113695743A US2013046033A1 US 20130046033 A1 US20130046033 A1 US 20130046033A1 US 201113695743 A US201113695743 A US 201113695743A US 2013046033 A1 US2013046033 A1 US 2013046033A1
Authority
US
United States
Prior art keywords
process according
iron
particles
nano
matrix
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
US13/695,743
Other languages
English (en)
Inventor
Cristina Ferrini
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.)
Casale SA
Original Assignee
Casale Chemicals SA
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 Casale Chemicals SA filed Critical Casale Chemicals SA
Assigned to CASALE CHEMICALS SA reassignment CASALE CHEMICALS SA ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: FERRINI, CRISTINA
Publication of US20130046033A1 publication Critical patent/US20130046033A1/en
Assigned to CASALE SA reassignment CASALE SA MERGER (SEE DOCUMENT FOR DETAILS). Assignors: AMMONIA CASALE SA, CASALE CHEMICALS SA, METHANOL CASALE SA, UREA CASALE SA
Abandoned legal-status Critical Current

Links

Classifications

    • 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
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0425—Catalysts; their physical properties
    • C07C1/043—Catalysts; their physical properties characterised by the composition
    • C07C1/0435—Catalysts; their physical properties characterised by the composition containing a metal of group 8 or a compound thereof
    • C07C1/044—Catalysts; their physical properties characterised by the composition containing a metal of group 8 or a compound thereof containing iron
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/02—Boron or aluminium; Oxides or hydroxides thereof
    • C07C2521/04—Alumina
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C07C2521/08—Silica
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/10—Magnesium; Oxides or hydroxides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/12—Silica and alumina
    • 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
    • C07C2523/74—Iron group metals
    • C07C2523/745—Iron
    • 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
    • C07C2523/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36
    • C07C2523/78—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups C07C2523/02 - C07C2523/36 with alkali- or alkaline earth metals or beryllium
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • the present invention relates to the production of light olefins, such as ethylene and propylene.
  • the present invention relates to a new process for preparing light olefins, such as C 2-4 olefins, with high yield and selectivity from synthesis gas.
  • Important sources of hydrocarbons for conversion include natural gas as well as refinery gases such as naphtha or other oil-based products.
  • light olefins such as C 2-4 olefins
  • C 2-4 olefins are produced by steam cracking or fluid catalytic cracking of cracker feedstocks composed of naphtha hydrocarbons.
  • the yield of light olefins, particularly of ethylene from a naphtha cracker depends upon the hydrocarbon content in the feed. Ethylene yields are highest when the feed is composed of high concentrations of paraffins, particularly linear paraffins. However, only limited supplies of highly linear paraffin feedstocks are available from petroleum refineries.
  • the syngas may be easily obtained from non oil-based sources, in particular natural gas which can be converted to syngas through conventional steam reforming processes.
  • the syngas can be converted to methanol through conventional processes and the resulting methanol can be transported to existing plants for light olefins production or used in an integrated plant for methanol and light olefins production, where methanol is converted into light olefin through conventional methanol to olefins (MTO) processes.
  • MTO methanol to olefins
  • MTO processes are also well known in art and usually allow to obtain light olefins, particularly ethylene and propylene with relativity high yield and high selectivity which can usually be more than 80%.
  • SAPOs silicolaluminophosphates
  • SAPO materials may be prepared by reacting appropriate sources of Al, Si and P in the presence of a structure-directing agent (template) under specific ratios and conditions.
  • template structure-directing agent
  • SAPO materials are highly critical. Sometimes, it is observed that, even using the same reactants, different materials may be obtained depending on the synthesis path used, these materials having same chemical composition and SAPO structure as identified by X-ray diffraction but different catalytic properties.
  • SAPO materials are costly due in particular to the high cost of the template, thereby the overall process for light olefins production starting from syngas and involving a MTO process is often not cost-effective compared to the conventional cracking processes of oil-based products such as naphtha.
  • the technical problem underlying the present invention is then that of providing a process for light olefin production from non-oil sources which allow to obtain light olefins with high yield and selectivity while involving low costs so as to be applicable to an industrial level.
  • a process for light-olefins production comprising the step of contacting syngas with a iron-based catalyst at a temperature in the range from 250° C. to 350° C., and at a pressure in the range from 10 bar to 40 bar.
  • light olefins means unsaturated hydrocarbons C2-C4, particularly ethylene and propene.
  • synthesis gas or syngas means a gas mixture mainly comprising CO and H2 obtained by conversion of non-oil sources.
  • the syngas may be obtained by converting natural gas through conventional steam reforming processes or by converting other non-oil sources, in particular coal or renewable sources such as biomass through conventional processes.
  • syngas it may be desirable to purify the syngas prior to the conversion to light olefins according to the invention to remove carbon dioxide produced during the syngas reaction, and any sulfur compounds, if they have not already been removed.
  • sulphur is a strong poison for the iron-based catalyst and should be removed as much as possible, for instance to a sulphur content in the syngas to be converted lower than 1 ppm.
  • a mildly alkaline solution e.g., aqueous potassium carbonate
  • the term “high selectivity” means a content of C 2-4 olefins, particularly ethylene and propylene, in gaseous reaction products obtained from the conversion of syngas on iron-based catalyst under the conditions of the invention, of at least 80% by weight, preferably 85-90% by weight.
  • the direct conversion of syngas to light olefins is carried out at a temperature in the range from 300° C. to 350° C. and at a pressure in the range from 10 bar to 40 bar.
  • the syngas may have a H2:CO molar ratio in the range from 1.5 to 2.5.
  • the syngas may contain up to 5.% of inert gaseous components.
  • the syngas has a H2:CO molar ratio around 2:1.
  • the first reaction is conventionally known as Fischer-Tropsch (FT) reaction but, as known in the art, it provides liquid fuels, such as gasoline (C 5 -C 11 ) and diesel (C 9 -C 25 ).
  • FT Fischer-Tropsch
  • grow chain in the FT reaction can be relatively low by using a iron-based catalyst in the FT reaction and operating the FT reaction at a temperature from 250° C. to 350° C. and at a pressure in the range from 10 bar to 40 bar. This advantageously allows to shift the selectivity of the syngas conversion towards light olefins.
  • such selectivity for light olefins is fully comparable to that obtained from MTO processes and it is at least 80% and preferably between 85% and 90%.
  • Iron-based catalysts are commonly used in ammonia synthesis processes from hydrogen and nitrogen as disclosed for example in the US patent application No.2009/0202417.
  • the catalyst includes iron and/or iron oxides particles as active component(s) which may be arranged on a metal oxide support or matrix.
  • Suitable metal oxide supports or matrices which can be used include alumina, titania, silica, magnesium oxide, silica-alumina, ferrous materials such as magnetite, wustite, cordierite and the like, and mixtures thereof.
  • the catalyst may also contain a promoter of the catalytic activity.
  • the promoter may be chosen from elements, molecules/compounds and combinations thereof including: aluminium, potassium, calcium, magnesium, silicon, manganese and copper.
  • the catalyst may comprise one or more promoters chosen from the list indicated above in a percentage of 0.1-5% by weight on the weight of the support or matrix. If the content of promoter(s) is less than 0.1%, the production of methane and paraffin may increase. In contrast, if the content of promoter(s) exceeds 5%, reaction activity and olefin yield are not significantly increased.
  • the most preferred promoters for catalylic activity used in the present invention are elements, molecules/compounds and combination thereof including manganese, potassium and copper.
  • potassium and copper promoters allows to increase adsorption of CO on the metal surface (the metal being iron (Fe) and/or iron oxides (FeOx)) providing an electron donor, thereby enhancing the grow chain reaction rate.
  • Manganese compounds in particular manganese oxide (MnO), are very useful as they increase the selectivity of the FT reaction to light olefins.
  • a particularly preferred iron-based catalyst including manganese (Mn) and potassium (K) promoters is particularly preferred in the process of the invention as it allows enhancing the selectivity for light olefins up to 85-90%.
  • the preparation of the iron-based catalyst used in the process according to the invention can be carried out by conventional processes normally used for preparing iron catalysts for ammonia synthesis. Such processes include precipitation of Fe particles onto the catalyst support or melting processes.
  • a suitable melting process involves melting of a Fe compound such as magnetite (Fe3O4) optionally with promoter compounds followed by cooling and solidification. The resulting porous material is then crushed into granules at the desired size. Active catalyst is then produced by reduction of iron oxides with hydrogen and nitrogen gas mixture, to give porous iron and unreduced promoter oxides.
  • Fe3O4 magnetite
  • promoter compounds optionally with promoter compounds followed by cooling and solidification.
  • Active catalyst is then produced by reduction of iron oxides with hydrogen and nitrogen gas mixture, to give porous iron and unreduced promoter oxides.
  • the size of the iron-based catalyst used in the present invention may be preferably in the range of 1-10 millimetres.
  • a particularly preferred catalyst includes nano-sized Fe particles as active component.
  • nano-sized Fe particles means Fe nano-particles, Fe alloy nano-particles, nano-particles having an iron or iron alloy core and an iron-oxide shell or mixtures thereof.
  • the content of nano-sized Fe particles is comprised between 1% and 5% by weight on the weight of the support or matrix.
  • the particles are preferably substantially spherical and have preferably a diameter less than about 50 nm, more preferably between about 15 and 25 nm, and most preferably between about 1 and 15 nm.
  • These particles can be produced through conventional processes for example by vapor condensation in a vacuum chamber as disclosed in the patent U.S. Pat. No. 7,282,167.
  • the nano-sized iron catalyst particles are disposed on a support material configured to disperse or separate the particles. In this way, iron sintering could be minimized and catalysis efficiency could be maintained over time.
  • the process according to the invention can be carried out in a variety of reactors for example, fixed bed reactors containing one or more catalyst beds, slurry reactors, fluidized bed reactors, or a combination of different type reactors.
  • the catalyst may also be activated prior to use in a conventional manner. This may be accomplished for example by reducing the catalyst under hydrogen atmosphere at 350-550° C. and normal pressure for 1-24 hours.
  • the process according to the invention may also include the step of removing the reaction heat in a continuous or discontinuous way. This may be accomplished by using reactors equipped with appropriate cooling means such as cooling plates internally crossed by a cooling fluid.
  • Direct conversion of syngas to light-olefins was performed using a catalyst containing nano-sized Fe particles dispersed on a matrix consisting of magnetite.
  • the percentage of nano-sized Fe particles was 1% by weight on the weight of the matrix (magnetite).
  • the nano-sized Fe particles were prepared according to the condensation process disclosed in U.S. Pat. No. 7,282,167. They comprised a Fe core and an iron-oxide coating and had average diameters from 15 to 25 nanometers.
  • the catalyst also contained 1% of Cu and 2% of K as promoters in percentages by weight on the weight of the support (magnetite).
  • the catalyst was introduced in a fixed bed reactor and then, under a condition of 320° C. and 20 bar, a syngas was flown at a SV (space velocity) of 500 vol./vol catalyst/hr.
  • reaction products were determined by sending the gaseous phase of a sample to a GC (gas chromathograph) after cooling and separation of the liquid phase.
  • the total amount of higher hydrocarbons in the liquid phase was determined by weighting.
  • the main reaction products were propene and ethylene.
  • the selectivity for C2-C4 light-olefins was about 85% while the CO conversion was about 92%.
  • the content of said promoters was 2% MnO and 2% of K in percentages by weight on the weigh of the matrix.
  • reaction products were determined by sending the gaseous phase of a sample to a GC (gas chromathograph) after cooling and separation of the liquid phase.
  • the total amount of higher hydrocarbons in the liquid phase was determined by weighting.
  • the main reaction products were propene and ethylene.
  • the selectivity for C2-C4 light-olefins was about 85% while the CO conversion was about 95%.
  • Direct conversion of syngas to light-olefins was performed using a catalyst containing Fe (non nano-sized) particles precipitated from an aqueous solution containing Fe (III) nitrate on a support (matrix) consisting of magnetite.
  • the catalyst also contained 2% of MnO and 2% of K as promoters in percentages by weight on the weight of the support (magnetite).
  • the catalyst was activated prior to use by reduction under hydrogen atmosphere at normal pressure and 480° C. for 12 hours and it was tested in the same way as example 1.
  • the main reaction products were propene and ethylene.
  • the selectivity for C2-C4 light-olefins was about 85% while the CO conversion was about 95%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)
  • Pharmaceuticals Containing Other Organic And Inorganic Compounds (AREA)
US13/695,743 2010-05-10 2011-05-06 Process for the Production of Light Olefins from Synthesis Gas Abandoned US20130046033A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP10162438.5 2010-05-10
EP10162438 2010-05-10
PCT/EP2011/057307 WO2011141374A1 (fr) 2010-05-10 2011-05-06 Procédé de production d'oléfines légères à partir de gaz de synthèse

Related Parent Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2011/057307 A-371-Of-International WO2011141374A1 (fr) 2010-05-10 2011-05-06 Procédé de production d'oléfines légères à partir de gaz de synthèse

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US14/510,899 Continuation US9139490B2 (en) 2010-05-10 2014-10-09 Process for the production of light olefins from synthesis gas

Publications (1)

Publication Number Publication Date
US20130046033A1 true US20130046033A1 (en) 2013-02-21

Family

ID=42813136

Family Applications (2)

Application Number Title Priority Date Filing Date
US13/695,743 Abandoned US20130046033A1 (en) 2010-05-10 2011-05-06 Process for the Production of Light Olefins from Synthesis Gas
US14/510,899 Active US9139490B2 (en) 2010-05-10 2014-10-09 Process for the production of light olefins from synthesis gas

Family Applications After (1)

Application Number Title Priority Date Filing Date
US14/510,899 Active US9139490B2 (en) 2010-05-10 2014-10-09 Process for the production of light olefins from synthesis gas

Country Status (14)

Country Link
US (2) US20130046033A1 (fr)
EP (2) EP3636626A1 (fr)
CN (1) CN102971277B (fr)
AU (1) AU2011252180B2 (fr)
BR (1) BR112012028846B1 (fr)
CA (1) CA2795553C (fr)
CL (1) CL2012002816A1 (fr)
DO (1) DOP2012000279A (fr)
EG (1) EG27128A (fr)
MX (1) MX341832B (fr)
MY (1) MY160507A (fr)
RU (1) RU2562459C2 (fr)
UA (1) UA111064C2 (fr)
WO (1) WO2011141374A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107824214A (zh) * 2017-11-10 2018-03-23 中石化炼化工程（集团）股份有限公司 一种合成气制取低碳烯烃的方法
US20220176365A1 (en) * 2019-03-29 2022-06-09 Exxonmobil Chemical Patents Inc. Supported Nanoparticle Compositions and Precursors, Processes for Making the Same and Syngas Conversion Processes
CN115555021A (zh) * 2022-10-04 2023-01-03 中国石油大学(华东) 一种二氧化碳加氢制液体烃联产低碳烯烃的催化剂制备方法

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014174372A2 (fr) 2013-04-24 2014-10-30 Saudi Basic Industries Corporation Production de produits à partir de ressources naturelles
CN104801304A (zh) * 2014-01-28 2015-07-29 中国科学院大连化学物理研究所 一种合成气制低碳烯烃的铁基催化剂及其制备和应用
CN106031871B (zh) * 2015-03-17 2018-10-19 中国科学院大连化学物理研究所 一种co2加氢制取低碳烯烃的铁基催化剂及其制备和应用
CN104907080B (zh) * 2015-05-18 2019-01-25 华东理工大学 一种铁基催化剂及其制备方法和应用
CN108144643B (zh) * 2016-12-05 2020-03-10 中国科学院大连化学物理研究所 一种催化剂及合成气直接转化制低碳烯烃的方法
CN108970600B (zh) * 2017-06-02 2021-01-19 中国科学院大连化学物理研究所 一种催化剂及合成气直接转化制低碳烯烃的方法
CN109704899B (zh) * 2017-10-26 2022-07-08 中国石油化工股份有限公司 合成气制备烯烃的方法
CN109939667B (zh) * 2018-01-26 2021-01-05 中国科学院大连化学物理研究所 一种催化剂及合成气直接转化制低碳烯烃的方法
CN115475626B (zh) * 2022-10-04 2023-11-17 中国石油大学(华东) 一种二氧化碳加氢制备长链烃联产低碳烯烃的催化剂制备方法
CN119608162B (zh) * 2024-12-30 2025-10-03 福州大学 一种用于合成氨的催化剂及其制备方法和应用

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011027921A2 (fr) * 2009-09-04 2011-03-10 Korea Research Institute Of Chemical Technology Catalyseur pour la production directe d'oléfines légères et son procédé de préparation

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4463101A (en) * 1980-12-29 1984-07-31 Mobil Oil Corporation Catalyst for converting synthesis gas to high octane predominantly olefinic naphtha
DE3130988A1 (de) * 1981-08-05 1983-02-24 Schering Ag, 1000 Berlin Und 4619 Bergkamen Katalysator und verfahren zur herstellung von olefinen - insbesondere linearen (alpha)-olefinen - aus synthesegas
CN1040397C (zh) * 1992-09-03 1998-10-28 中国科学院大连化学物理研究所 合成气制低碳烯烃含铁锰催化剂及合成反应
DE69615557T2 (de) * 1995-06-29 2002-04-18 Sasol Technology (Proprietary) Ltd., Johannesburg Verfahren zur herstellung von sauerstoff enthaltenden verbindungen
US6534552B2 (en) * 1998-03-31 2003-03-18 Rentech, Inc. Producing liquid hydrocarbons from natural gas
WO2001089686A2 (fr) * 2000-05-23 2001-11-29 Sasol Technology (Proprietary) Limited Produits chimiques provenant de gaz de synthese
CN1309477C (zh) * 2002-05-15 2007-04-11 苏德-化学股份公司 用高纯度铁前体制备的费－托催化剂
US7282167B2 (en) 2003-12-15 2007-10-16 Quantumsphere, Inc. Method and apparatus for forming nano-particles
CN101396662A (zh) * 2007-09-28 2009-04-01 北京化工大学 一种用于合成气制低碳烯烃的纳米催化剂及制备方法
KR100904297B1 (ko) * 2007-10-26 2009-06-25 한국화학연구원 연속적인 2단계 촉매 반응을 이용한 합성가스로부터 경질올레핀의 제조방법
US20090202417A1 (en) 2007-11-06 2009-08-13 Quantumsphere, Inc. System and method for ammonia synthesis
KR100962181B1 (ko) * 2008-04-28 2010-06-10 한국화학연구원 피셔-트롭쉬 합성용 철계 촉매 및 이의 제조방법

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2011027921A2 (fr) * 2009-09-04 2011-03-10 Korea Research Institute Of Chemical Technology Catalyseur pour la production directe d'oléfines légères et son procédé de préparation

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Zhang et al., CHEMICAL ABSTRACT CN 101396662, APRIL 2009. *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107824214A (zh) * 2017-11-10 2018-03-23 中石化炼化工程（集团）股份有限公司 一种合成气制取低碳烯烃的方法
US20220176365A1 (en) * 2019-03-29 2022-06-09 Exxonmobil Chemical Patents Inc. Supported Nanoparticle Compositions and Precursors, Processes for Making the Same and Syngas Conversion Processes
US11857954B2 (en) * 2019-03-29 2024-01-02 Exxonmobil Chemical Patents Inc. Supported nanoparticle compositions and precursors, processes for making the same and syngas conversion processes
CN115555021A (zh) * 2022-10-04 2023-01-03 中国石油大学(华东) 一种二氧化碳加氢制液体烃联产低碳烯烃的催化剂制备方法

Also Published As

Publication number Publication date
RU2562459C2 (ru) 2015-09-10
BR112012028846B1 (pt) 2018-06-19
UA111064C2 (uk) 2016-03-25
MY160507A (en) 2017-03-15
RU2012152820A (ru) 2014-06-20
CL2012002816A1 (es) 2013-03-22
CN102971277A (zh) 2013-03-13
CA2795553C (fr) 2019-09-24
EP3636626A1 (fr) 2020-04-15
MX341832B (es) 2016-09-02
BR112012028846A2 (pt) 2016-07-26
CA2795553A1 (fr) 2011-11-17
AU2011252180A1 (en) 2012-11-01
AU2011252180B2 (en) 2016-05-19
EP2569266B1 (fr) 2020-01-22
MX2012012980A (es) 2012-12-17
CN102971277B (zh) 2015-12-02
WO2011141374A1 (fr) 2011-11-17
EP2569266A1 (fr) 2013-03-20
US20150025160A1 (en) 2015-01-22
US9139490B2 (en) 2015-09-22
EG27128A (en) 2015-07-22
DOP2012000279A (es) 2013-04-15

Similar Documents

Publication Publication Date Title
US9139490B2 (en) Process for the production of light olefins from synthesis gas
JP5411133B2 (ja) 二酸化炭素の合成ガスへの接触水素化
RU2450044C2 (ru) Способ активации катализатора синтеза фишера-тропша
CA3030838C (fr) Carbure de molybdene dope avec un metal alcalin supporte sur de l'alumine gamma pour l'hydrogenation selective de co2 en co
AU2003295625B2 (en) Process for the preparation of linear alpha-olefins from synthesis gas over a cobalt catalyst
WO2008134484A2 (fr) Catalyseur et procédé pour la conversion du gaz naturel en des composés de plus haute masse moléculaire
JP2024535794A (ja) 二酸化炭素含有原料からの液化石油ガス（ｌｐｇ）炭化水素の製造
Speight Liquid fuels from natural gas
Luo et al. Effect of palladium on iron Fischer–Tropsch synthesis catalysts
WO2017085603A2 (fr) Procédés pour la conversion de co2 en gaz de synthèse utile dans la production d'oléfines
KR101600139B1 (ko) 천연가스를 이용한 경질 올레핀의 제조 방법
CN113574009A (zh) 由通过催化部分氧化结合裂化制得的合成气生产甲醇的方法
US20230340334A1 (en) Processes for the production of liquid fuels from carbon containing feedstocks, related systems and catalysts
JP2011084528A (ja) プロピレンの製造方法
CN109158107B (zh) 一种由二氧化碳直接加氢制备液体烃的方法
Hayakawa et al. Studies on catalytic performance of precipitated iron/silica catalysts for Fischer–Tropsch Synthesis
Zaman et al. Syngas to lower olefins over bulk Mo2N catalysts prepared with citric acid
McGregor 21 Fischer–Tropsch synthesis using CO2
Vosoughi DEVELOPMENT OF SUPPORTED COBALT CATALYST FOR FISCHER-TROPSCH SYNTHESIS
RU2205171C1 (ru) Способ получения длинноцепочечных углеводородов из co и h2 в жидкой фазе
AU2019309214B2 (en) Fluidized bed processes and catalyst systems for fischer-tropsch conversion
Seby Effect of Promoter (Mn) on the Performance of SBA-15 Supported Iron Catalysts forHigh Temperature Fischer-Tropsch Synthesis
Ma Direct Synthesis of Gasoline from Syngas on Hybrid Catalyst
WO2018088986A1 (fr) Procédés de production de combustibles liquides à partir de charges d'alimentation contenant du carbone, systèmes et catalyseurs associés
KR20140080920A (ko) 합성가스로부터 저급 탄화수소 화합물 제조용 촉매 및 이의 제조방법

Legal Events

Date Code Title Description
AS Assignment

Owner name: CASALE CHEMICALS SA, SWITZERLAND

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:FERRINI, CRISTINA;REEL/FRAME:029240/0977

Effective date: 20121002

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION

AS Assignment

Owner name: CASALE SA, SWITZERLAND

Free format text: MERGER;ASSIGNORS:AMMONIA CASALE SA;UREA CASALE SA;METHANOL CASALE SA;AND OTHERS;REEL/FRAME:034533/0456

Effective date: 20140527