Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
  • C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
  • C01B3/326—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents characterised by the catalyst
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
  • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
• • 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
  • B01J23/54—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals combined with metals, oxides or hydroxides provided for in groups B01J23/02 - B01J23/36
  • B01J23/56—Platinum group metals
  • B01J23/63—Platinum group metals with rare earths or actinides
• • 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
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
  • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
  • C01B3/382—Multi-step processes
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
  • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
  • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
  • C01B3/40—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B32/00—Carbon; Compounds thereof
  • C01B32/40—Carbon monoxide
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
  • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/02—Processes for making hydrogen or synthesis gas
  • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
  • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
  • C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1041—Composition of the catalyst
  • C01B2203/1047—Group VIII metal catalysts
  • C01B2203/1064—Platinum group metal catalysts
  • C01B2203/107—Platinum catalysts
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/10—Catalysts for performing the hydrogen forming reactions
  • C01B2203/1041—Composition of the catalyst
  • C01B2203/1082—Composition of support materials
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
  • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
  • C01B2203/1205—Composition of the feed
  • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
  • C01B2203/1217—Alcohols
  • C01B2203/1229—Ethanol
• • 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 invention relates to a method for cleaving ethanol in d-blocks in a pre-reformer and a suitable catalyst.
• Fuel cells allow an efficient and environmentally friendly conversion of chemical into electrical energy. Due to the direct conversion, a high electrical efficiency with low emissions is achieved. Fuel cells have the potential to become an important technology of the future both in the stationary (as combined heat and power) and in the mobile (transport) or portable electricity generation (as a replacement for today's batteries and accumulators).
• the fuel cell represents a special form of a galvanic element.
• the electrical energy is obtained by the chemical reaction of hydrogen with oxygen to water, whereby the cell works silently and without mechanical wear.
• the fuels do not belong directly to the cell and can be supplied continuously.
• fossil and renewable fuels such as natural gas, biogas or methanol can also be converted.
• the Polymer Electrolyte Membrane Fuel Cell is much more sensitive to contamination than, for example, Molten Carbonate Fuel Cell (MCFC) or Solid Oxide Fuel Cell (SOFC).
• MCFC Molten Carbonate Fuel Cell
• SOFC Solid Oxide Fuel Cell
• the temperature is so low that no appreciable levels of NO x , for example, are produced.
• the fuel cell consists of the fuel electrode (anode), the electrolyte and the air-oxygen electrode (cathode).
• the different fuel cells can be divided into different types. The subdivision can take place either via the different electrolytes (melt, polymer membrane or solid oxide) or else through the different operating temperatures (low, medium or high temperature) of the fuel cells. In the area of lower performance, the low-temperature fuel sites, which include the hydrogen-fueled PEMFC, dominate.
• the PEMFC, Direct Methanol Fuel Cell (DMFC) and Phosphoric Acid Fuel Cell (PAFC) are based on the transport of protons through an acidic electrolyte.
• the SOFC and MCFC require high temperatures in order to achieve a sufficient ionic conductivity of the solid electrolyte.
• the high working temperature of 650 ° C at the MCFC enables not only the production of electricity and heat but also the generation of steam. This can either drive a downstream steam turbine, which increases the electrical efficiency, or be used directly in industrial plants as process steam. Due to the high working temperature in the cell, the reforming of natural gas to hydrogen and carbon dioxide can take place internally. An external reformer is not necessary.
• the high temperatures and the aggressive liquid salts (alkali carbonates) of the electrolyte make high demands on the material.
• the MCFC operates at a temperature range that allows for partial reforming of methane in the presence of a suitable catalyst.
• DIR direct internal reforming
• NR indirect internal reforming
• the reforming catalyst is located in the anode compartment, while it is located in the NR between the cells in the stack.
• Ni-based catalyst it would be rapidly poisoned by the DIR in an MCFC through contact with the carbonate-containing electrolyte.
• the different arrangement in the NR bypasses this direct contact and thus increases the life of the catalyst considerably.
• the waste heat generated by the MCFC can be utilized by the internal reforming process and the efficiency of the fuel cell can be increased.
• ethanol is to be used as fuel for a fuel cell, in particular a melted carbonate fuel cell (MCFC)
• the ethanol must first be split in a pre-reformer so that Cr building blocks such as methane, CO and CO 2 -containing fuel gas are obtained, that of the fuel cell is supplied.
• the catalyst used should at the same time be selective in order to prevent the formation of by-products such as acetaldehyde, ethene or the like, which could damage the fuel cell, in particular the molten carbonate fuel cell.
• it should advantageously be possible to operate at a low S / C ratio (steam / carbon ratio) in order to enable economical operation.
• the object of the present invention is to provide a catalyst and a method for cleaving ethanol into d-blocks in a pre-reformer, meeting the above requirements.
• the object is achieved by a method for cleaving ethanol nol in d-blocks in a pre-reformer, in which ethanol and steam are reacted at a temperature in the range of 300 to 550 0 C on a catalyst, the platinum on a mixture comprising ZrO 2 and CeO 2 carrier.
• d-blocks molecules resulting from cleavage of the carbon-carbon bond in ethanol.
• the main d building blocks are methane, CO and CO 2 .
• These Cr blocks differ, for example, from C 2 compounds formed as by-products during cleavage, such as acetaldehyde and ethene, or resulting solid carbon, which can inactivate the catalyst as a result of deposit formation and whose formation must therefore be avoided.
• the Prereformer can be, for example, a steam reformer (Dampfprereformer).
• platinum as an active metal makes it unnecessary to reduce the catalyst, as is necessary, for example, in the case of nickel, so that a corresponding hazard potential is avoided and the start of the reaction is simplified. Low platinum contents allow for economical catalyst production.
• ethanol When ethanol is split in the pre-reformer, ethanol is converted with water to methane, carbon monoxide, carbon dioxide and hydrogen. Carbon monoxide can in turn be converted with water to carbon dioxide and hydrogen.
• the direct dehydration of ethanol in ethene and water should be avoided as much as the formation of carbon.
• a catalyst comprising platinum on a carrier containing a mixture of ZrC> 2 and CeC> 2 is particularly suitable for steam reforming of ethanol.
• ZrC> 2 and CeC> 2 are used as mixed powder or as co-precipitation, so that no specific mixed oxide or redox mixed oxide is present, but ZrO 2 and CeO 2 are present side by side, in contrast to, for example, the cited reference from Applied Catalysis b, according to which obviously a mixed oxide is used.
• the catalyst preferably contains from 0.1 to 5% by weight of platinum, based on the total catalyst, and the weight ratio of CeO 2 to ZrO 2 is from 1: 2 to 1: 7.
• the amount of platinum is particularly preferably 0.15 to 1 wt .-%, in particular 0.2 to 0.5 wt .-%, especially about 0.25 wt .-%.
• the weight ratio of CeO 2 to ZrO 2 is particularly preferably 1: 3 to 1: 6, in particular 1: 4 to 1: 5, in particular about 1: 4.5.
• the amount of platinum is preferably 0.1 to 0.5 wt .-%, particularly preferably 0.15 to 0.5 wt .-%, in particular 0.2 to 0.5 wt .-% , based on the total weight of the catalyst.
• the weight ratio of CeO 2 to ZrO 2 can be generally freely selected.
• the catalyst can have exclusively ZrC> 2 and CeC> 2 as carrier material.
• the catalyst can only have platinum as the active metal, so that it consists of platinum, ZrO 2 and CeO 2 , apart from excipients.
• the catalyst is doped with 0.01 to 10 wt .-%, particularly preferably 1 to 8 wt .-%, in particular 3 to 6 wt .-%, based on the total weight of the catalyst, of at least one rare earth metal oxide.
• the rare earth metal is preferably lanthanum, yttrium or praseodymium. Particularly preferred is lanthanum.
• the catalyst preferably additionally contains from 3 to 20% by weight, more preferably from 5 to 15% by weight, in particular from 7 to 12% by weight, based on the total weight of the catalyst, of Al 2 O 3 .
• the BET surface area of the oxidic powder used for the carrier preparation is preferably 50 to 150 m 2 / g, more preferably 70 to 110 m 2 / g.
• the BET surface area is preferably increased by about 10 m 2 / g.
• the total area of the pores in the finished catalyst is preferably 60 to 120 m 2 / g, particularly preferably 70 to 110 m 2 / g, in particular 80 to 95 m 2 / g.
• metal oxides may be present as additives in the catalyst support, for example alkali metal oxides and metal oxides of group VIII of the Periodic Table of the Elements, in particular iron oxide.
• the preparation of the catalyst can be carried out by any suitable method, which can be chosen depending on the desired shape.
• the catalyst support can be prepared, for example, by co-precipitation from a solution. Alternatively, it may be prepared by kneading the oxides of the catalyst support, followed by shaping, drying and calcining.
• the active metals in particular platinum, can be applied in the form of an aqueous salt solution before or after the preparation of the catalyst support.
• a finished catalyst support can be impregnated with a platinum salt solution, dried and calcined. It is also possible to add an aqueous platinum salt solution before kneading.
• the preparation of the catalyst is carried out by kneading CeO 2 , ZrO 2 , optionally Al 2 O 3 and, if present, rare earth metal oxide with addition of water, subsequent shaping, drying and calcining, wherein an aqueous platinum salt solution is added before kneading or applied after drying.
• the catalyst can be used in the process according to the invention in any suitable form, for example in the form of powders, spun, granules, pellets, tablets or extrudates.
• the catalyst is preferably used in strand form as a fixed bed.
• the process for reforming ethanol can be carried out continuously or batchwise. Preferably, it is carried out continuously.
• the resulting gas mixture can be fed to a reformer, wherein also preforming and reforming can be provided as interconnected apparatus units.
• a reformer wherein also preforming and reforming can be provided as interconnected apparatus units.
• the further reaction takes place in a fuel cell, in particular a Molten Carbonates Fuel Cell (MCFC).
• MCFC Molten Carbonates Fuel Cell
• the reaction is carried out at a temperature in the range of 300 to 550 0 C, preferably at 350 to 525 0 C, in particular at 400 to 500 0 C.
• the pressure can be chosen freely.
• the absolute pressure is often 0.5 to 20 bar, preferably 0.8 to 2.0 bar, in particular 1, 2 to 1, 5 bar.
• the molar ratio S / C of water vapor to C atoms in the pre-reformer is preferably in the range from 1.8 to 5.9, particularly preferably 2.0 to 4.0, in particular 2.2 to 3.0.
• the GHSV (Gas Hourly Space Velocity) is frequently 500 to 10,000 h -1 , preferably at most 4500 h -1 and at least 2000 h -1 .
• the upper limit is 4000 h -1 , particularly preferably 3000 h -1 , especially preferably 2500 h "1 .
• Ethanol can be used in any suitable form in the process.
• bio-ethanol can be used, as well as ethanol / methanol mixtures, which can also contain water in small quantities. Small amounts of formic acid and aldehydes can be tolerated, preferably these compounds are not present.
• the proportion of methanol, based on the alcohols in the mixture, is preferably not more than 20% by weight, more preferably not more than 10% by weight.
• the gas mixture obtained from the pre-reformer contains preferably at an S / C value of 2.5 to 3.0, 5 to 45 vol .-% hydrogen, 0 to 80 vol .-% nitrogen, 0 to 3 vol .-% carbon monoxide , 2 to 25 vol.% Methane, 2 to 25 vol.% Carbon dioxide, the total amount being 100 vol.%.
• S / C value 2.5 to 3.0, 5 to 45 vol .-% hydrogen, 0 to 80 vol .-% nitrogen, 0 to 3 vol .-% carbon monoxide , 2 to 25 vol.% Methane, 2 to 25 vol.% Carbon dioxide, the total amount being 100 vol.%.
• the impregnation with the desired amount of a 12.9 wt .-% platinum nitrate solution is carried out in a trough drum using a spray nozzle.
• the strands are placed in the impregnating drum and sprayed with stirring with the platinum nitrate solution.
• DA after dried at 200 0 C for 4 hours and then calcined at 500 0 C for 2 hours.
• the resulting catalyst has a bulk density of 1093 g / l.
• the CeO 2 / ZrO 2 / La 2 O 3 powder (80 wt% ZrO 2 , 13 wt% CeO 2 , 7 wt% La 2 O 3 ) is added in an amount of 1289 , 3 g together with 183.65 g of Al 2 O 3 (Pural ® SB) presented in a kneader. Then dilute hydrochloric acid and water are added and 26.6 g of platinum nitrate solution (12.9 wt .-% strength). A total of 59.5 g of 65% HNO 3 was added. The total amount of water added was 530 ml. It was kneaded for 10 minutes and enough water was added to form a plastic mass. The plastic mass was deformed at the extruder to 1.5 mm diameter strands at a pressure of 85 to 95 bar after a preliminary kneading time of 80 minutes.
• the resulting catalyst has a bulk density of 1120 g / l.
• CeO 2 ZZrO 2 ZLa 2 O 3 can be kneaded with Al 2 O 3 , and Pt-SaIz and HNO 3 can be introduced into the kneading. Then it is extruded, dried and cal- cinated. It is also possible to place the Pt salt on the carrier.
• Example 2 60 ml of the catalyst from Example 2 were incorporated into the reactor. Subsequently, the catalyst was covered with a layer of quartz wool (about 10 to 15 ml). At the beginning of the testing, the reactor was brought under nitrogen (100 Nits) to the starting temperature (see table) and a pressure of 2.5 bar absolute.
• the preheating temperature of the feed was set at 300 0 C to 500 0 C.
• the start temperature (between 450 to 550 0 C) of the reactor was reached, the nitrogen was fueling closed and started the water dosing. After another 5 minutes, the experiment was started by the start of the ethanol dosage.
• the load (GHSV) was 2500 h -1 at an SZC ratio of 2.5 to 3.0
• the evaluation of the test data was carried out with the aid of the GC exhaust gas data from the reactor and the measurement data from the Dasylab data acquisition software (Version 5.6 ).

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• 2009
  • 2009-04-21 US US12/988,727 patent/US20110036012A1/en not_active Abandoned
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