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%.

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• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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• 2011
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