WO2008079052A1 - Catalyseur de synthèse fischer-tropsch et procédé de production associé - Google Patents

Catalyseur de synthèse fischer-tropsch et procédé de production associé Download PDF

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Publication number
WO2008079052A1
WO2008079052A1 PCT/RU2007/000693 RU2007000693W WO2008079052A1 WO 2008079052 A1 WO2008079052 A1 WO 2008079052A1 RU 2007000693 W RU2007000693 W RU 2007000693W WO 2008079052 A1 WO2008079052 A1 WO 2008079052A1
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Prior art keywords
catalyst
oxide
carbon fiber
carrier
weight
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PCT/RU2007/000693
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English (en)
Russian (ru)
Inventor
Vladimir Zalmanovich Mordkovich
Yanina Vladislavovna Mikhailova
Sergei Alexandrovich Svidersky
Lilia Vadimovna Sineva
Igor Grigorevich Solomonik
Vadim Sergeevich Ermolaev
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Limited Liability Company 'syntop'
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Publication of WO2008079052A1 publication Critical patent/WO2008079052A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • B01J23/46—Ruthenium, rhodium, osmium or iridium
    • B01J23/462—Ruthenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/18—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/75—Cobalt
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
    • B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
    • B01J23/889—Manganese, technetium or rhenium
    • B01J23/8896—Rhenium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
    • C10G2/331—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing group VIII-metals

Definitions

  • the invention relates to petrochemistry, gas chemistry, coal chemistry and relates to a Fischer-Tropsch synthesis catalyst and a method for producing said catalyst.
  • the Fischer-Tropsch synthesis proceeds in the presence of catalysts based on metals of group VIII of the Periodic Table of Mendeleev.
  • the composition of the catalyst determines the composition of the resulting products.
  • the Fischer-Tropsch process is exothermic and proceeds at elevated pressures.
  • To maintain the high activity and selectivity of the catalysts in this reaction, such an optimization of its composition is necessary that would reduce the likelihood of overheating. Overheating negatively affects the selectivity of the catalyst with respect to the formation of the target products, leading to the predominant reaction of direct hydrogenation of CO in methane and deactivation of the catalyst [B. Jaeger, R. Escopoza Advapses Ip-tempter-Tsslacto, 1995. , v.23, p. 17-28].
  • the process is carried out in liquid phase conditions.
  • the liquid phase plays the role of a reaction and heat transfer medium at the same time, and the catalyst in the form of a suspension is distributed in the liquid phase.
  • a solid catalyst in the form of granules, rings, etc., forming a fixed layer is placed inside a tube separating the gas space from the catalyst and the liquid phase (water), by heating which heat is removed.
  • the thermal conductivity of the solid catalyst plays a large role in the removal of heat.
  • a cobalt catalyst for the Fischer-Tropsch synthesis is known [US Patent Application US 2003/139286 Al (2003)].
  • the catalyst is cobalt supported on a carbon-coated oxide carrier (Al 2 O 3 , SiO 2 , aluminosilicate, TiO 2 , MgO).
  • a carbon-containing carrier is prepared as described in European patent EP 0681868 Al (1995). The carbon content is from 0.1 g per 100 g of the carrier to 40 g per 100 g of the carrier.
  • the catalyst is prepared by co-impregnating solutions of cobalt salts and a metal promoter in a slarry reactor, followed by drying in a rotary evaporator under vacuum and calcining in air for 6 hours at 250 ° C.
  • the catalyst is partially reduced in a current. hydrogen for 2 hours at 230 ° C. Then carry out the following joint impregnation with drying and calcination.
  • the use of such a carrier improves the stability of the catalyst in a three-phase reactor.
  • the disadvantage of this catalyst is the complexity of the preparation.
  • Known catalyst for Fischer-Tropsch synthesis [International patent application WO 86/01499 Al], representing cobalt or iron deposited on a carrier, which is carbon which has a specific surface area of at least 100 m 2 / g.
  • the ratio of the total specific surface determined by BET to the specific surface of the main plane should not exceed 4: 1, and the ratio of the specific surface of the main plane to the specific surface of the side plane should be at least 10: 1.
  • the catalyst also contains a promoter - platinum (0.2-10 wt.%).
  • the catalyst is prepared by impregnation of carbon powder (0.5-1.0 mm) with aqueous solutions of metal salts.
  • carbon from organic materials is treated sequentially in an inert, oxidizing and again inert atmosphere at temperatures from 300 to 3300 ° C.
  • the synthesis is carried out at 150-300 ° C, 0.1-5 MPa and a ratio of H 2 / CO - 1 / 1-3 / 1.
  • the disadvantages of this catalyst include low selectivity for C 5+ products.
  • a known catalyst for the synthesis of hydrocarbons from synthesis gas [RF Patent SU 1819158 AZ (1990)].
  • the catalyst contains iron as an active component, copper, silicon and potassium, and activated carbon or mineral acid coal
  • coal particles (2-20 wt.%). Moreover, 50-100% of coal particles have a value of 0.1-100 microns.
  • Fischer-Tropsch is carried out in a reactor with a fixed catalyst bed at a pressure of 20-30 bar and a temperature of 220-320 ° C.
  • the yield of hydrocarbon wax is 40-55% in terms of hydrocarbons C 2 and C 2+ .
  • the disadvantages of this catalyst are its low productivity and selectivity for the target products, as well as a complex method of preparation.
  • the closest is a cobalt catalyst for the synthesis of hydrocarbons
  • C 5 -C 25 from CO and H 2 based on activated carbon (content - 20-90 wt.%) Obtained from almond bark, coconut, palm tree or coal (US Patent No. 6720283 (2004)).
  • the support is characterized by a surface area of 200-2000 m 2 / g, a pore volume of 0.3-2 ml / g and a pore diameter of 4 to 1000 A.
  • the catalyst is prepared by impregnating the support powder (20-40 mesh) with solutions of Co, Zr or Ce nitrates in vacuum (80 kPa), followed by drying at room temperature for several days, drying at 80-90 ° C for 8 hours and at 110-120 0 C for 10 hours.
  • the problem solved by the claimed inventions is to create a highly efficient Fischer-Tropsch synthesis catalyst with increased activity and selectivity for high molecular weight hydrocarbons by increasing its thermal conductivity, as well as a method for producing a catalyst.
  • the catalyst for Fischer-Tropsch synthesis contains, as an active component, a metal of group VIII of the Periodic Table of D. I. Mendeleev and a carrier containing an oxide component and carbon fiber.
  • the use of carbon fiber in the preparation of the carrier allows to increase the thermal conductivity of the granules, and, consequently, the thermal stability of the catalyst layer as a whole. Since the synthesis of hydrocarbons from CO and H 2 proceeds with a large heat release, properly organized heat removal of the reaction allows increasing the productivity and selectivity of the catalyst for target products at least 1.5 times. At the same time, the selectivity of the formation of the main by-product, methane, decreases by more than 3 times.
  • the content of the active component may be 5-40% by weight of the catalyst. At a lower content of the active component, the reaction rate decreases to values that do not justify the use of a catalyst for the synthesis of hydrocarbons according to the Fischer-Tropsch method. An increase in the active metal content above 40% is not justified from an economic point of view.
  • the oxide component may comprise alumina and / or silica and / or titanium oxide and / or zirconium oxide.
  • the catalyst may contain promoters, which can be used zirconium metal or metals of groups VII or VIII of the Periodic Table of D. I. Mendeleev and / or their oxides, while the content of promoters is 0.1-5% by weight of the catalyst.
  • promoters can be used zirconium metal or metals of groups VII or VIII of the Periodic Table of D. I. Mendeleev and / or their oxides, while the content of promoters is 0.1-5% by weight of the catalyst.
  • the use of promoters also contributes to an increase in activity, productivity and selectivity of the catalyst.
  • Carbon fiber can be used in the form of segments of a length of not more than 3 mm and a diameter of not more than 20 microns, preferably a diameter of not more than 10 microns and a length of up to 2 mm. Such dimensions of the carbon fiber provide a fairly tight contact with the particles of the oxide carrier and with each other, which creates the most favorable conditions for heat transfer in the catalyst granule.
  • the carbon fiber may have a specific surface area of not higher than 800 m 2 / g. This allows you to further increase the selectivity of the formation of the target product, by reducing the possibility of the formation of additional centers of hydrogenation of CO in the by-product of the synthesis - methane.
  • the carbon fiber content is 1-25% by weight of the catalyst. This content is optimal for combining the influence of two factors:
  • the carbon fiber segments may be in the form of a cylinder. This allows you to further increase the performance of the catalyst by improving the thermal conductivity of the granules, making the heat sink directional.
  • the method of producing the catalyst for the Fischer-Tropsch synthesis consists in the fact that the active component is applied by impregnation on a carrier, which is prepared from paste by extrusion, the extrudates are held in air, dried and calcined, while the paste used contains an oxide component, a plasticizer, carbon fiber and a binder.
  • the carbon fiber content may be 1-25% by weight of the catalyst. This content is optimal for combining the influence of two factors: on the one hand, it is enough to increase the thermal conductivity of the catalyst granules, and on the other hand, it is not enough to adversely affect the strength of such a granule.
  • Alumina and / or silicon oxide and / or titanium oxide and / or zirconium oxide can be used as the oxide component.
  • boehmite can be used in an amount of 5-15% by weight of the catalyst.
  • the paste may also contain a pore-forming component.
  • the introduction of the active component can be carried out by impregnating the formed support with a solution of salts of the corresponding metals to its content of 5-40% by weight of the catalyst.
  • Promoters can be introduced into the carrier by impregnating the carrier with a solution of their salts to a content of 0.1-5% by weight of the catalyst.
  • the catalyst preparation method proposed in the present invention consists in preparing a paste containing an oxide component, carbon fiber, a boehmite binder, water, a plasticizer and its extrusion, drying and calcining, after which sequential stages of impregnation with metal salt solutions are carried out for 5–40 wt.% cobalt and, if necessary, 0.1-5% of the promoter with intermediate stages of drying and calcination.
  • a carrier is prepared in the first stage of preparation of the catalyst.
  • the carbon fiber (UB), the oxide component of the carrier, boehmite and, if necessary, the pore-forming component with distilled water, nitric acid and a plasticizer to a paste-like state, extrude it, hold it in air for 8-15 hours, and dry it in an oven at 60 -110 0 C and calcined in a stream of inert gas at 110-550 ° for 6-20 hours.
  • the active component (cobalt) is applied by impregnation in several stages from a solution of cobalt salt (nitrate, acetate, formate, acetylacetonate, etc.).
  • the sample is dried in a water bath and the resulting catalyst precursor is dried and / or calcined in an inert gas stream at a temperature of 100 to 1000 ° C for 0.5-10 hours. If necessary, a metal or oxide promoter is introduced in a similar manner.
  • the catalyst sample is activated by reduction in a stream of hydrogen (bulk velocity 100-5000 h "1 ) at a temperature of 300-600 ° C for 0.5-5 hours.
  • the synthesis of hydrocarbons from CO and H 2 is carried out in a tubular reactor with a stationary catalyst bed at a pressure of 0.1-4 MPa and a temperature of 150-300 ° C.
  • the molar ratio of CCVH 2 in the synthesis gas is 1 / 1-3.
  • the synthesis gas may contain up to 25 vol.% Nitrogen.
  • a sample of the catalyst composition 30% Co / (Al 2 Oz + 25% YB) is prepared in the following way.
  • Dried extrudates are loaded into a flowing quartz reactor and calcined in a stream of nitrogen, raising the temperature from PO to 550 ° C at a speed 3-4 ° C / min. It is kept at a temperature of 55 ° C for 5 hours.
  • the extrudates are cooled in a stream of nitrogen, discharged from the reactor and crushed to a fraction of 2.5x2-3 mm.
  • Cobalt is applied from an aqueous solution of its nitrate in three consecutive impregnations.
  • the catalyst sample is activated in a stream of hydrogen (about 3,000 h "1 ) at 450 ° C for 1 h.
  • a sample of the catalyst composition 30% Co / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • a mixture of 0.45 ml of HNO 3 (64%), 8 ml of distilled water and 0.6 g of triethylene glycol plasticizer (TEG) is added to 2 g of boehmite SB-I. Mix thoroughly until smooth. To the mixture add 2 g of carbon fiber powder and mix thoroughly until smooth. Next, 6 g of Al 2 O 3 powder is added to the mixture, mixed thoroughly until smooth and placed in an extruder with a 2.5 mm die. The extrudates are held in air for 10 hours and placed in an oven. Drying mode in an oven: 60 ° C - 2 h, 80 0 C - 2 h, 110 ° C - 2 h.
  • TOG triethylene glycol plasticizer
  • Dried extrudates are loaded into a flowing quartz reactor and calcined in a stream of nitrogen, raising the temperature from PO to 550 ° C at a speed 3-4 ° C / min. They stand for 5 hours at 550 ° C.
  • the extrudates are cooled in a stream of nitrogen, discharged from the reactor and crushed to a fraction of 2.5x2-3 mm. Cobalt is applied as in example 1.
  • a sample of the catalyst composition 30% Co / (Al 2 O 3 + 7% UB) is prepared in the following way.
  • a mixture of 0.45 ml of HNO 3 (64%), 8 ml of distilled water and 0.6 g of triethylene glycol plasticizer (TEG) is added to 2 g of boehmite SB-I. Mix thoroughly until smooth.
  • To the mixture add 1 g of carbon fiber powder and mix thoroughly until smooth.
  • 7 g of Al 2 O 3 powder is added to the mixture, mixed thoroughly until smooth and placed in an extruder with a 2.5 mm die. The extrudates are held in air for 10 hours and placed in an oven.
  • Drying mode in an oven 60 0 C - 2 h, 80 ° C - 2 h, HO 0 C - 2 h.
  • Dried extrudates are loaded into a flowing quartz reactor and calcined in a stream of nitrogen, raising the temperature from 110 to 550 0 C at a speed 3-4 ° C / min. It is kept at a temperature of 55 ° C for 4 hours.
  • the extrudates are cooled in a stream of nitrogen, discharged from the reactor, and crushed to a fraction of 2.5 x 2-3 mm.
  • Cobalt is applied as in example 1.
  • Example 4 A sample of the catalyst composition 30% Co / (Al 2 O 3 + 1% UB) is prepared in the following way.
  • a mixture of 0.45 ml of HNO 3 (64%), 8 ml of distilled water and 0.6 g of triethylene glycol plasticizer (TEG) is added to 2 g of boehmite SB-I. Mix thoroughly until smooth. To the mixture add 0.15 g of carbon fibers and mix thoroughly until smooth. Next, 7.85 g of Al 2 O 3 powder is added to the mixture, mixed thoroughly until smooth and placed in an extruder with a 2.5 mm die. The extrudates are held in air for 10 hours and placed in an oven. Drying mode in an oven: 60 ° C - 2 hours, 80 0 C - 2 hours, 11O 0 C - 2 hours.
  • the dried extrudates are loaded into a flowing quartz reactor and calcined in a stream of nitrogen, raising the temperature from 110 to 550 0 C at a speed 3-4 ° C / min. It is held at 550 ° C for 4 hours.
  • the extrudates are cooled in a stream of nitrogen, discharged from the reactor and crushed to a fraction of 2.5x2-3 mm.
  • Cobalt is applied as in example 1.
  • a catalyst sample of 10% Co / (Al 2 O 3 + 25% UB) was prepared in the following manner.
  • the media is prepared as in example 1.
  • Cobalt is applied from an aqueous solution of its nitrate. 7.05 g of cobalt nitrate is dissolved in distilled water and added to 10 g of the obtained carrier. The mixture is placed in a porcelain cup and dried in a water bath for 30-60 minutes.
  • a sample of the catalyst composition 30% Co-0, l% Re / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2.
  • Cobalt is applied from an aqueous solution of its nitrate, and rhenium from ammonium perrenate in four consecutive impregnations.
  • Example 7 A catalyst sample of 30% Co-0.5% Re / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2.
  • Cobalt and rhenium are applied, as in example 4.
  • a sample of the catalyst composition 30% Co-0.5% Pt / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2.
  • Cobalt and platinum are applied as in example 4. Activation of the catalyst and synthesis is carried out as in example 1. Example 9.
  • a sample of the catalyst composition 30% Co-5% ZrO 2 / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2.
  • Cobalt and zirconium oxide are applied as in Example 7.
  • a sample of the catalyst composition 30% Co-3% Fe 2 O 3 / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2.
  • Cobalt and iron oxide are applied as in example 7.
  • Example 11 A sample of the catalyst composition 30% Co / (TiO 2 + 14% UB) is prepared in the following way.
  • a mixture of 0.45 ml of HNO 3 (64%), 8 ml of distilled water and 0.6 g of triethylene glycol plasticizer (TEG) is added to 2 g of boehmite SB-I. Mix thoroughly until smooth. To the mixture add 2 g of carbon fibers and mix thoroughly until smooth. Next, 6 g of TiO 2 powder is added to the mixture, mixed thoroughly until smooth and placed in an extruder with a 2.5 mm die. The extrudates are held in air for 10 hours and placed in an oven. Drying mode in an oven: 60 0 C - 2 h, 8O 0 C - 2 h, 110 0 C - 2 h.
  • TOG triethylene glycol plasticizer
  • Dried extrudates are loaded into a flowing quartz reactor and calcined in a stream of nitrogen, raising the temperature from 110 to 550 0 C at a speed 3-4 ° C / min. It is held for 4 hours at a temperature of 550 ° C.
  • the extrudates are cooled in a stream of nitrogen, discharged from the reactor and crushed to a fraction of 2.5x2-3 mm.
  • Cobalt is applied as in example 1.
  • a sample of the catalyst composition 30% Fe / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the media is prepared as in example 2. Iron is applied from an aqueous solution of its nitrate in three successive impregnations.
  • the catalyst sample is activated in a stream of hydrogen (about 3,000 h "1 ) at 450 0 C for 1 h.
  • a sample of the catalyst composition 30% Ru / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the carrier is prepared, as in example 2. Ruthenium is applied from an aqueous solution of its chloride in three consecutive impregnations.
  • a sample of the catalyst composition 30% Co-0.5% Re / (Al 2 O 3 + 14% UB) is prepared in the following way.
  • the carrier is prepared as in example 2. Cobalt and rhenium are applied as in example 4.
  • the activation of the catalyst is carried out as in example 1.
  • a catalyst sample of 30% Co / Al 2 O 3 was prepared in the following manner.
  • Cobalt is applied, as in example 1.
  • Activation of the catalyst and synthesis is carried out, as in example 1.
  • the invention relates to petrochemistry, gas chemistry and can be used for Fischer-Tropsch synthesis.

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Abstract

La présente invention relève de la pétrochimie et de la chimie du gaz et du charbon, et concerne un catalyseur de synthèse Fischer-Tropsch ainsi qu'un procédé de production dudit catalyseur. Le catalyseur Fischer-Tropsch selon l'invention contient un composant actif se présentant sous la forme d'un métal du groupe VIII du tableau périodique de Mendeleïev, et un support contenant un élément oxyde et une fibre de carbone. Le procédé de production du catalyseur selon l'invention consiste : à appliquer par imprégnation le composant actif sur le support, lequel est obtenu par extrusion à partir d'une pâte; à maintenir les extrudats à l'air; à les sécher et à les calciner. La pâte utilisée contient un élément oxyde, un liant, un plastifiant et une fibre de carbone. L'invention permet d'obtenir un catalyseur sélectif et très efficace.
PCT/RU2007/000693 2006-12-27 2007-12-11 Catalyseur de synthèse fischer-tropsch et procédé de production associé WO2008079052A1 (fr)

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RU2006146573/04A RU2325226C1 (ru) 2006-12-27 2006-12-27 Катализатор для синтеза фишера-тропша и способ его получения

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20120214664A1 (en) * 2009-10-29 2012-08-23 Infra Technologies Ltd. Catalyst for synthesis of hydrocarbons from co and h2 and preparation method thereof
US8445550B2 (en) 2010-11-23 2013-05-21 Chevron U.S.A. Inc. Ruthenium hybrid fischer-tropsch catalyst, and methods for preparation and use thereof
WO2021026346A1 (fr) * 2019-08-06 2021-02-11 Kemira Oyj Compositions et procédés de traitement des eaux usées

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RU2685437C2 (ru) * 2017-05-26 2019-04-18 ИНФРА ИксТиЭл ТЕКНОЛОДЖИ ЛИМИТЕД Катализатор для синтеза фишера-тропша и способ получения этого катализатора

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US8865613B2 (en) * 2009-10-29 2014-10-21 Infra XTL Technology Limited Catalyst for synthesis of hydrocarbons from CO and H2 and preparation method thereof
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WO2021026346A1 (fr) * 2019-08-06 2021-02-11 Kemira Oyj Compositions et procédés de traitement des eaux usées

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