Classifications

• • 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
  • B01J23/80—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 zinc, cadmium or mercury
• • 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
  • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
  • B01J21/04—Alumina
• • 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
  • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
  • B01J27/24—Nitrogen compounds
  • B01J27/25—Nitrates
• • 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
  • B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
  • B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
  • B01J31/04—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing carboxylic acids or their salts
• • 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
  • 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
  • C07C41/09—Preparation of ethers by dehydration of compounds containing hydroxy groups
• • 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
  • B01J23/72—Copper

Definitions

• the invention relates to a catalytically active body for the synthesis of dimethyl ether from synthesis gas.
• the invention relates to an improved catalytically active body for the synthesis of dimethyl ether, whereby the components of the active body comprise a defined particle size distribution.
• the present invention concerns a method for the preparation of a catalytically active body, the use of the catalytically active body and a method for preparation of dimethyl ether from synthesis gas.
• Hydrocarbons are essential in modern life and used as fuel and raw materials, including the chemical, petrochemical, plastics, and rubber industry.
• Fossil fuels such as oil and natural gas are composed of hydrocarbons with a specific ratio of carbon to hydrogen.
• fossil fuels also have limitations and disadvantages in the view of being a finite resource and their contribution to global warming if they are burned.
• DME dimethyl ether
• Methanol can be converted into DME by dehydration over an acidic catalyst.
• reaction (1 ) reaction (1 ) and reaction (2), are listed below.
• Reaction (1 ) occurs with the combination of three reactions, which are Methanol synthesis reaction, Methanol dehydration reaction, and water gas shift reaction:
• reaction (1 ) has a stoichiometric ratio H 2 /CO of 1 :1 and has some advantages over reaction (2).
• reaction (1 ) generally allows higher single pass conversions and less energy-consuming in comparison to the removal of water from the system in reaction (2).
• the document US 6,608,1 14 B1 describes a process for producing DME by dehydrating the effluent stream from the methanol reactor, where the methanol reactor is a slurry bubble column reactor (SBCR), containing a methanol synthesis catalyst that con- verts a synthesis gas stream comprising hydrogen and carbon monoxide into an effluent stream comprising methanol.
• SBCR slurry bubble column reactor
• Document WO 2008/157682 A1 provides a method of forming dimethyl ether by bimo- lecular dehydration of methanol produced from a mixture of hydrogen and carbon diox- ide, obtained by reforming methane, water, and carbon dioxide in a ratio of about 3 to 2 to 1. Subsequent use of water produced in the dehydration of methanol in the bi- reforming process leads to an overall ratio of carbon dioxide to methane of about 1 :3 to produce dimethyl ether.
• Document WO 2009/0071 13 A1 describes a process for the preparation of dimethyl ether by catalytic conversion of synthesis gas to dimethyl ether comprising contacting a stream of synthesis gas, comprising carbon dioxide with one or more catalysts active in the formation of methanol and the dehydration of methanol to dimethyl ether, to form a product mixture comprising the components dimethyl ether, carbon dioxide and uncon- verted synthesis gas, washing the product mixture comprising carbon dioxide and unconverted synthesis gas in a first scrubbing zone with a first solvent rich in dimethyl ether and subsequently washing the effluent from the first scrubbing zone in a second scrubbing zone with a second solvent rich in methanol to form a vapor stream comprising unconverted synthesis gas stream with reduced content of carbon dioxide transfer- ring the vapor stream comprising unconverted synthesis gas stream with reduced carbon dioxide content for the further processing to dimethyl ether.
• the US 6,191 ,175 B1 describes an improved process for the production of methanol and dimethyl ether mixture rich in DME from essentially stoichiometrically balance synthesis gas by a novel combination of synthesis steps.
• the present invention relates to a catalyst used for producing dimethyl ether comprising a methanol synthesis catalyst produced by adding one or more promoters to a main catalyst comprised of a Cu-Zn-AI metal component and a dehydration catalyst formed by mixing Aluminium Phosphate (AIP0 4 ) with gamma alumina, a method of producing the same, and a method of producing dimethyl ether using the same, wherein a ratio of the main catalyst to the promoter in the methanol synthesis catalyst in a range of 99/1 to 95/5, and a mixing ratio of the methanol synthesis catalyst to the dehydration catalyst is in a range of 60/40 to 70/30.
• AIP0 4 Aluminium Phosphate
• the object of the present invention is to provide a catalytically active body that shows the ability to convert CO-rich synthesis gas selectively into dimethyl ether and C0 2 , whereby ideally the yield of the DME is increased in comparison to the state of the art. If the conversion is incomplete, the resulting off-gas comprises hydrogen and carbon monoxide preferably in the ratio H 2 /CO ⁇ 1. Thus the off-gas can be recycled directly after the separation of the product DME and C0 2 .
• a catalytically active body for the synthesis of dimethyl ether from synthesis gas comprising a mixture of:
• component (B) 10-30 % by weight of an acid component, selected from the group consisting of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ - aluminiumoxide with 0.1-20 % by weight of Niobium, Tantalum, Phosphorus or Boron, related to component (B), or mixtures thereof,
• the ternary oxide is a zinc-aluminium-spinel.
• (A) 70-90 % by weight of a methanol-active component, selected from the group consisting of copper oxide, aluminium oxide, zinc oxide, amorphous aluminium oxide, ternary oxide or mixtures thereof, whereby the component (A) has a particle size distribution characterized by a D-10 value of 5-140 pm, a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm,
• component (B) 10-30 % by weight of an acid component, selected from the group consisting of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ - aluminiumoxide with 0.1-20 % by weight of Niobium, Tantalum, Phosphorus or Boron, related to component (B), or mixtures thereof, whereby the component (B) has a particle size distribution characterized by a D-10 value of 5-140 pm, a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm,
• This particle size distribution can be determined via state of the art analysis techniques, e.g. via analysis apparatus like Mastersizer 2000 or 3000 by Malvern Instruments GmbH.
• the particle size distribution in the sense of the invention is characterized by the D10-, D50-, and D-90 value.
• D10 is: that equivalent diameter where 10 mass % (of the particles) of the sample has a smaller diameter and hence the remaining 90% is coarser.
• D50 and D90 can be derived similarly (see: HORIBA Scientific, A Guidebook to Particle Size Analysis" page 6)
• the inventive catalytically active body is characterized by a high turnover of carbon monoxide, preferably at 180°C to 350°C and particular at 200°C to 300°C.
• a suitable pressure for the synthesis of DME is preferably in the range from 20 to 80 bar and in particular from 30 to 50 bar.
• the components (A) or (B) have a particle size distribution characterized by a D-10, D-50, and D-90 value of 5-80 pm, 40-270 pm, and 250-800 pm respectively.
• the particle size distribution from component (A) can be different from component (B).
• the components (A) or (B) have a particle size distribution characterized by a D-10, D-50, and D-90 value of 5-50 pm, 40-220 pm, and 350- 800 ⁇ respectively.
• the particle size distribution from component (A) can be different from component (B).
• a catalytically active body can be a body known in the art that contains pores or channels or other features for enlargement of surface, which will help to bring the educts in contact that they can react to the desired product.
• a catalytically active body in the sense of the present invention can be understood as a physical mixture, whereby the components (A) and (B) contact each other and presenting channels and/or pores between their contact surfaces. Preferably, the components (A) and (B) are not melted or sintered at their contact surfaces.
• a methanol-active component in the sense of the present invention is a component which leads to the formation of methanol, starting from hydrogen, carbon monoxide or carbon dioxide or mixtures thereof.
• the methanol-active compound is a mix- ture of copper oxide, aluminium oxide and zinc oxide, whereby copper oxide can consist of all kinds of oxides of copper.
• copper has the oxidation state (I) or (II) in the oxide.
• the aluminium oxide according to the present invention can also be referred to ⁇ -alumina or corundum, whereby zinc in zinc oxide in the sense of the present invention preferably has the oxidation state (II).
• the component (B) is aluminium oxide hydroxide and ⁇ -aluminiumoxide in a ratio of 3:7 to 6:4, preferably in a ratio of 1 :2 to 5:4, whereby the ratio is by weight.
• Component (B) is selected from the group consists of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ -aluminiumoxide with 0.1-20 % by weight of Niobium, Tantalum, Phosphorus or Boron, or mixtures thereof, related to component (B).
• component (B) is of selected from the group consisting of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ -aluminiumoxide with 1-10 % by weight of Niobium, Tanta- lum, Phosphorus, or Boron, related to component (B).
• the component (A) comprises 50-80 % by weight of copper oxide, 15-35 % by weight of ternary oxide and 15-35 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 65-75 % by weight of copper oxide, 20-30 % by weight of ternary oxide and 20-30 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 50-80 % by weight of copper oxide, 2-8 % by weight of boehmite and 15-35 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 65-75 % by weight of copper oxide, 3-6 % by weight of boehmite and 20-30 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 50-80 % by weight of copper oxide, 2-8 % by weight of amorphous aluminium oxide and 15-35 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 65-75 % by weight of copper oxide, 3-6 % by weight of amorphous aluminium oxide and 20-30 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 50-80 % by weight of copper oxide, 2-8 % by weight of aluminium oxide and 15-35 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• the component (A) comprises 65-75 % by weight of copper oxide, 3-6 % by weight of aluminium oxide and 20-30 % by weight of zinc oxide and the sum of which is in total 100 % by weight.
• component (B) has a surface area from 70-270 m 2 /g with a pore volume in the range from 0.35-0.1.45 ml/g, preferably a surface area from 85-220 m 2 /g with a pore volume in the range from 0.35- 1.35 ml/g and in particular a surface area from 1 10-200 m 2 /g with a pore volume in the range from 0.51-1.14 ml/g.
• the catalytically active body component (B) is boehmite, preferably a boehmite containing mineral.
• Boehmite occurs in tropical laterites and bauxites developed on alumino-silicate bedrock. It also occurs as a hydrothermal alteration product of corundum and nepheline. It occurs with kaolinite, gibbsite and diaspore in bauxite deposits and with nepheline, gibbsite, diaspore, natrolite and analcime in nepheline pegmatites.
• an additive (C) can be a structure-promoter like but not limited a thermally decomposable compound like polymers, wood dust, flour, graphite, film material, a painting, straw, strearic acid, palmitic acid, celluloses or a combination thereof.
• the structure-promotor can help to build up pores or channels.
• the catalytically active body is a pellet with a size in the range from 1 x 1 mm to 10 x 10 mm, preferably in the range from 2 x 2 mm to 7 x 7 mm.
• the pellet is obtained by pressing the mixture of the components (A), (B) and (C) to a pellet.
• a pellet can be obtained by pressing the components (A), (B) and optionally (C) under force to the pellet, whereby the shape of the pellet can be ring-shaped, star-shaped or spherical-shaped.
• the pellet can be hollow strings, triloops, multihole pellets, extrudates and alike.
• the present invention further relates to a method for the preparation of a catalytically active body, comprising the step: preparing a physical mixture comprising:
• a methanol-active component selected from the group consisting of copper oxide, aluminium oxide, zinc oxide, amorphous aluminium oxide, ternary oxide or mixtures thereof,
• an acid component selected from the group consisting of aluminium hydroxide, aluminium oxide hydroxide and/or y- aluminiumoxide with 0.1-20 % by weight of Niobium, Tantalum, Phosphorus or Boron, related to component (B), or mixtures thereof,
• preparing a physical mixture means that the different compounds (A), (B) and (C) are brought in contact without further chemical modification.
• the component (A) has a particle size distribution characterized by a D-10 value of 5-80 pm, a D-50 value of 40-270 pm, and a D- 90 value of 250-800 pm
• the component (B) has a particle size distribution characterized by a D-10 value of 5-80 pm, a D-50 value of 40-270 pm, and a D-90 val- ue of 250-800 pm and the particle size distribution of components (A) and (B) being maintained in the catalytically active body.
• the component (A) has a particle size distribution characterized by a D-10 value of 5-50 pm, a D-50 value of 40-220 pm, and a D-90 value of 350-800 pm
• the component (B) has a particle size distribution characterized by a D-10 value of 5-50 pm, a D- 50 value of 40-220 pm, and a D-90 value of 350-800 pm and the particle size distribution of components (A) and (B) being maintained in the catalytically active body.
• the method comprising further the steps: a) precipitation a copper-, zinc- or aluminium salt or a mixture thereof, b) calcination of the product obtained in step a),
• step c) calcination of a salt comprising Niobium, Tantalum, Phosphorus or Boron with a mixture of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ - aluminiumoxide
• the steps a), b) and c) are carried out before the step d).
• the salt further comprises oxalate, acetate and acetylacetonate.
• the obtained product consists after step d) of 70-90 % by weight of a meth- anol-active component (A), selected from the group consisting of copper oxide, alumin- ium oxide and zinc oxide or mixtures thereof, 10-30 % by weight of an acid component (B), selected from the group consists of aluminium hydroxide, aluminium oxide hydroxide and/or ⁇ -aluminiumoxide with 0.1-20 % by weight of Niobium, Tantalum, Phosphorus or Boron, related to component (B), or mixtures thereof.
• A meth- anol-active component
• B an acid component
• the component (A) has a particle size distribution characterized by a D-10 value of 5-140 pm, a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm and the component (B) has a particle size distribution characterized by a D-10 value of 5-140 pm, a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm.
• the method comprises at least spray drying, filtration, grinding, sieving or further steps, known in the art to create a catalytically active body, or combinations thereof.
• precipitation is a method for the formation of a solid in a solution or inside another solid during a chemical reaction or by diffusion in a solid.
• the precipitation techniques are known in the art, see also Ertl, Gerhard, Knozinger, Helmut, Schuth, Ferdi, Weitkamp, Jens (Hrsg.) "Handbook of Heterogeneous Catalysis” 2nd edition 2008, Wiley VCH Weinheim, Vol. 1 , chapter 2.
• salts of copper, zinc or aluminium are dissolved in a solvent, in particular water.
• At least two of the salts of either copper, zinc, or aluminium can be dissolved in a solvent, heated and a basic solution can be prepared and added. Both solutions can be added in parallel to the template, till the salt-solution is consumed. After this the suspension is vacuumed, dried, and calcinated under air flow.
• Preferred anions in the salts for copper, zinc, or aluminium are selected from the group consisting of, nitrate, acetate, carbonate, halide, nitrite, sulfate, sulfite, sulfide, phosphate ion or silicate.
• salts of copper, zinc or aluminium formed with the above mentioned anions can be converted into oxides of copper, zinc or aluminium applying a calcination step.
• Calcination in the sense of the present invention can be understood as a thermal treatment process applied to ores and other solid materials to bring about a thermal decomposition, phase transition, or removal of a volatile fraction.
• the calcination process normally takes place at temperatures below the melting point of the product materials. Usually it is done under oxygen-containing atmosphere. In some cases the calcination can be performed under inert atmosphere (e.g. nitrogen).
• preparing a physical mixture means that the different compounds (A), (B) and (C) are bringing in contact without further chemical modification.
• the components (A), (B) and (C) can be compacted in a presser, a squeezer, a crusher or a squeezing machine, preferably after step a), b), c) or d).
• Compacting in the sense of the present invention can mean that particles of a defined particle size distribution are pressed to bodies, which have a diameter in the range of 1 to 10 mm and a height of 1 to 10 mm. Preferably the particle size distribution is still left after the compacting.
• a pellet is formed, preferably with a size in the range from 1 x 1 mm to 10 x 10 mm, especially in the range from 2 x 2 mm to 7 x 7 mm.
• the components (A) and (B) independently pressed through at least one sieve, whereby the sieve exhibits a mesh size from 0.005 to 5 mm in order to obtain a particle size distribution characterized by a D-10 value of 5-140 pm, a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm.
• the sieve exhibits a mesh size from 0.005 to 1.50 mm and in particular a mesh size from 0.005 to 0.8 mm.
• the particles can also exhibit particle size distribution characterized by a D-10, D-50, and D-90 value of 5-140 pm, 40-300 pm, and 180-800 pm respectively.
• the components (A) and (B) can be obtained as particles with a defined particle size distribution, also referred in the sense of the present invention as a split-fraction. Because of this split-fraction the CO-conversion increases when synthesis gas contacts the split-fraction. Furthermore the yield of the DME increases, when synthesis gas is converted to DME by the catalytically active body. Preferably, this step is included in step d).
• component (C) is admixed to the components (A) and (B) before sieving.
• At least three different sieves are used, whereby the components (A) and (B) are pressed in direction from the sieve with the biggest mesh size to the sieve with the smallest mesh size.
• the components (A) and (B) are initially pressed into the sieve with the biggest mesh size, which results in particles with the maximal size of the mesh size of this sieve.
• the particle size distribution of the components (A) and (B) is characterized by a D-10 value of 5-140 ⁇ , a D-50 value of 40-300 pm, and a D-90 value of 180-800 pm. These particles can also be broken during the first sieving, so that smaller particles are obtained, which can go through the second sieve, which exhibits a smaller mesh size. Therefore a first fraction with a parti- cle size distribution can be obtained before the second sieve. This fraction can also be used as a catalytically active body.
• the particles which go through the second sieve with a mesh size smaller than the first sieve, but bigger than the third sieve, can be obtained behind the second sieve and before the smallest sieve with the smallest mesh size.
• the particles obtained after the second (middle) sieve can be used as a catalytically active body.
• the particles obtained after the sieve with the biggest mesh size could be pressed through the second sieve in order to reduce the particle size.
• step a) at least a part of the component (A) is prepared by precipitation reaction and/or calcination.
• precursors of the component (A) in form of a salt in a solution can be heated and adjusted to a defined pH-value.
• a calcination step can be carried out, whereby calcination is known from prior art.
• At least one part of component (A) is precipitated and whereby at least another part of component (A), which is not subjected to the first precipitation, is added to the precipitate.
• it is added by spray drying or precipation.
• the method further comprises the step e) adding a mixture of hydrogen and nitrogen to component (A) and/or (B).
• the content of the volume of the hydrogen is less than 5% in the mixture.
• the present invention further relates to a method for the preparation of dimethyl ether from synthesis gas comprising at least the steps: f) reducing the catalytically active body
• the method comprising the steps: h) providing the inventive catalytically active body, in particular in form of pellets i) filling the catalytically active body in a reactor,
• the present invention further relates to the use of a catalytically active body according to the present invention for the preparation of dimethyl ether. Preferred admixtures and preferred methods for the preparation a mentioned above and also included in the use.
• Solution 1 A solution of 1.33 kg copper nitrate, 2.1 kg zinc nitrate and 0.278 kg aluminium nitrate are solved in 15 L water.
• Solution 2 2.344 kg sodium bicarbonate is dissolved in 15 L water.
• Solution 1 A solution of 2.66 kg copper nitrate, 1.05 kg zinc nitrate and 0.278 kg aluminium nitrate are solved in 15 L water.
• Solution 2 2.344 kg sodium bicarbonate is dissolved in 15 L water.
• An impregnated solution is prepared that consists of 0.5 g ammonium niobate(V) oxalate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AbCVAIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 2 g ammonium niobate(V) oxalate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 4 g ammonium niobate(V) oxalate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 03/AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying ofen. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5 0 C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 6 g ammonium niobate(V) oxalate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use. Synthesis of an AlgOVAIOOH-mixture doped with niobium (8.16 % by weight)
• An impregnated solution is prepared that consists of 16 g ammonium niobate(V) oxalate dissolved in 100 ml water.
• An 40 g AI 2 03/AIOOH-mixture crushed extrudates con- sisting of 60 % gamma- Al 2 0 3 and 40% boehmite
• the suspension is exhausted by a Nutsche Filter.
• this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 2.61 g samarium(lll)-acetate hydrate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room tern Synthesis of an A Og/AIOOH-mixture doped with tin (2.04 % by weight)
• An impregnated solution is prepared that consists of 2.39 g tin(ll)-acetate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 03/AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 1.25 g ammonium metatungstate hydrate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 03/AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 3.59 g yttrium(lll) acetate hydrate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g Al 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 2.72 g cerium(lll) acetate hydrate and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 6.86 g boric acid and 27.4 ml de- mineralised water. With spray-watering this solution is applied onto 40 g AI 2 O 3 AIOOH- mixture (crushed extrudates consisting of 60 % gamma- AI2O3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use. Synthesis of an AlpOg/AIOOH-mixture doped with gallium (2.04 % by weight)
• An impregnated solution is prepared that consists of 6.32g gallium(lll) acetylacetonat and 27.4 ml demineralised water. With spray-watering this solution is applied onto 40 g AI 2 0 3 /AIOOH-mixture (crushed extrudates consisting of 60 % gamma- Al 2 0 3 and 40% boehmite). Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450 D C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• An impregnated solution is prepared that consists of 4.00 g ammonium niobate(V) oxalate and 20.9 ml demineralised water. With spray-watering this solution is applied onto 40 g Plural SCF 55. Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room tem- perature the material is ready for use. Synthesis of AI 2 Q 3 doped with niobium (2.04 % by weight on Pluralox SCF A230)
• An impregnated solution is prepared that consists of 4.00 g ammonium niobate(V) oxalate and 25.6 ml demineralised water. With spray-watering this solution is applied onto 40 g Pluralox SCF A230. Afterwards this material is dried for 12 h and 90 °C in the drying oven. After drying the material is calcinated in a rotating tube for 3 h at 450°C under nitrogen atmosphere (30nl/h). The heating rate is 5°C/min. After cooling to room temperature the material is ready for use.
• the methanol-active compound and the acid compound are compacted separately in a tablet press and/or pelletizing machine.
• the catalytically active body (5 cm 3 by volume) is incorporated in a tubular reactor (inner diameter 0.4 cm, bedded in a metal heating body) on a catalyst bed support consisting of alumina powder as layer of inert material and is pressure-less reduced with a mixture of 1 Vol.-% H 2 and 99 Vol.-% N 2 .
• the temperature is increased in intervals of 8 h from 150°C to 170°C and from 170°C to 190°C and finally to 230°C.
• the synthesis gas is introduced and heated within 2h up to 250°C.
• the synthesis gas consists of 45% H 2 and 45% CO and 10% inert gas (argon).
• the catalytically active body is run at an input temperature of 250°C, GHSV of 24001V 1 and a pressure of 50 bar.
• Tests for pelletized materials are conducted in a similar test rick compared to the setup described above for non-pelletized materials using the same routine. Only nojubular reactor with an inner diameter of 0.4 cm is used but a tubular reactor having an inner diameter of 3 cm. Tests for pelletized materials are done with a catalyst volume of 100 cm 3 . Results:
• e30 Consists of 70% by weight of CuO, 5,5% by weight Al 2 0 3 and 24,5% by weight of ZnO.
• table 1 the results are presented.
• Me30 and D10-21 mixture from boehmite and gamma-Alox in a ratio of 4:6), Pluralox and Plural are used.
• compositions of the catalytically active body show differ- ent CO-conversions.
• the comparison experiments C1 to C9 showing a lower turnover, whereby the inventive experiments V1 to V9 showing an increased value.
• Olethers are compounds that are formed out of H 2 and CO in the reactor that are not MeOH, DME, or C0 2 .

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• 2013
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