US20070129243A1 - Catalyst and sorbent material for the production of hydrogen - Google Patents

Catalyst and sorbent material for the production of hydrogen Download PDF

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Publication number
US20070129243A1
US20070129243A1 US11/621,142 US62114207A US2007129243A1 US 20070129243 A1 US20070129243 A1 US 20070129243A1 US 62114207 A US62114207 A US 62114207A US 2007129243 A1 US2007129243 A1 US 2007129243A1
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shell
core
catalyst
pellets
hydrogen
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US11/621,142
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Thomas Wheelock
Brent Shanks
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Iowa State University Research Foundation ISURF
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Iowa State University Research Foundation ISURF
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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
    • B01J23/70—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
    • B01J23/78—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 alkali- or alkaline earth metals
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B01J20/041—Oxides or hydroxides
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/06—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04
    • B01J20/08—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising oxides or hydroxides of metals not provided for in group B01J20/04 comprising aluminium oxide or hydroxide; comprising bauxite
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/28—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties
    • B01J20/28014—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof characterised by their form or physical properties characterised by their form
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/3078—Thermal treatment, e.g. calcining or pyrolizing
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
    • B01J20/3202—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating characterised by the carrier, support or substrate used for impregnation or coating
    • B01J20/3204—Inorganic carriers, supports or substrates
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/30—Processes for preparing, regenerating, or reactivating
    • B01J20/32—Impregnating or coating ; Solid sorbent compositions obtained from processes involving impregnating or coating
    • B01J20/3291—Characterised by the shape of the carrier, the coating or the obtained coated product
    • B01J20/3293—Coatings on a core, the core being particle or fiber shaped, e.g. encapsulated particles, coated fibers
    • 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
    • B01J37/0203—Impregnation the impregnation liquid containing organic compounds
    • 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
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
    • C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
    • 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
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • B01J2220/00—Aspects relating to sorbent materials
    • B01J2220/40—Aspects relating to the composition of sorbent or filter aid materials
    • B01J2220/48—Sorbents characterised by the starting material used for their preparation
    • B01J2220/4875—Sorbents characterised by the starting material used for their preparation the starting material being a waste, residue or of undefined composition
    • B01J2220/4887—Residues, wastes, e.g. garbage, municipal or industrial sludges, compost, animal manure; fly-ashes
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/396—Distribution of the active metal ingredient
    • B01J35/397—Egg shell like
    • 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
    • B01J37/0205—Impregnation in several steps
    • 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
    • B01J37/16—Reducing
    • 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
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/0425—In-situ adsorption process during hydrogen production
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/1235—Hydrocarbons
    • C01B2203/1241—Natural gas or methane
    • 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

  • This invention relates to a pelletized material having an absorbent core encased in a strong but porous shell having catalytic properties.
  • a material is preferred for industrial chemical processes which produce hydrogen and carbon dioxide. These processes include the steam reforming of hydrocarbons and processes based on the water gas shift reaction.
  • Hydrogen is an important raw material in the chemical and petroleum industries. Large quantities are used in the manufacture of ammonia and methanol and in a variety of petroleum hydrotreating processes.
  • methane is the principal component of natural gas and may be plentiful, it can also be produced by hydrogasification of coal.
  • the primary method for converting methane and other light hydrocarbons to produce hydrogen is based on steam reforming.
  • the steam methane reforming (SMR) process often involves multiple steps and severe operating conditions, including high temperatures and pressures.
  • SERP Sorption Enhanced Reaction Process
  • Membrane-based reaction systems may involve the use of metallic membranes which only small molecules like hydrogen can permeate, or polymeric, ceramic, and zeolitic membranes.
  • the membranes may act as permselective barriers, or as an integral part of the catalytically active surface.
  • the present inventors have now discovered a unique method of producing hydrogen through the reaction of steam with methane, other light hydrocarbons, or carbon monoxide using a catalyst and sorbent combined in the same pelletized material.
  • the method is unique compared to presently available technology in that it does not require the catalytic reforming and product separation steps to be conducted with different materials in completely separate steps.
  • the invention describes a catalyst and sorbent in pellet form wherein each pellet combines a reactive core with a porous protective shell having a catalyst embedded or coated on the surface of the pores of the shell.
  • Such materials are useful for various hydrogen manufacturing processes, and specifically for catalytically reforming methane or other hydrocarbon gases to produce hydrogen and carbon dioxide while at the same time separating the hydrogen from the carbon dioxide.
  • the core-in-shell catalyst and sorbent of this invention includes a core of reactive, but comparatively physically weak, material and a strong but porous shell with catalytic properties.
  • the shell maintains the structural integrity of the catalyst and sorbent during its use.
  • the sorbent is also preferably able to retain its structural integrity during numerous cycles of use and regeneration.
  • the core is made of any material which will absorb or react with carbon dioxide (CO 2 ) in order to remove it from the H 2 -containing product.
  • the shell of the sorbent is a material which gives the pellet sufficient strength while allowing CO 2 gas to penetrate to (diffuse to) the sorbent material in the core.
  • the successful protective layer (shell) can be largely refractory cement or alumina.
  • Preferred materials for the preparation of CaO cores include powdered limestone, dolomite, and plaster of Paris.
  • Types I, III, and IV Portland cement, high alumina cement (HAC), and calcium aluminate refractory cement can be used as shell materials. These are hydraulic cements which require curing.
  • An alternative shell material is comprised of a sinterable powder (e.g., alumina) which upon heat treatment forms a strong, porous shell.
  • core and shell raw materials which are appropriate for use in this invention include, but are not limited to, the following: Core material: Shell material: CaO (lime & swollen lime) Bentonite clay CaCO 3 (limestone, swollen Attapulgite clay limestone) CaCO 3 •MgCO 3 (dolomite) Zeolite material MgO Portland cements SrO High temperature refractory cement BaO Alumina Fly ash Calcium aluminates Magnesium oxysulfate cement
  • CaO.MgO derived from dolomite may also be possible to use as a core material for removing CO 2 from gas produced by gasifying coal. In this respect, it is believed the following reaction takes place: CaO.MgO (s) +CO 2(g) CaCO 3 .MgO (s)
  • MgO does not participate in the reaction, it serves to maintain the structural integrity and chemical reactivity of the sorbent.
  • the core-in-shell concept is not limited to the specifically-listed materials above.
  • the concept can be applied to other absorbent materials which lack the necessary strength and durability in themselves to withstand repeated loading and regeneration.
  • the effects of loading and regeneration can be particularly severe where the sorbent is converted from one chemical species to another during loading and then is converted back to the original species during regeneration.
  • Such changes are accompanied by changes in the physical structure of the material which can produce changes in the specific volume of the material. Repeated swelling and shrinking of the material as it is loaded and regenerated can weaken the material and lead to spalling and disintegration. This type of failure has been observed with zinc-based sorbents for H 2 S where the material undergoes significant changes in specific volume during regeneration.
  • the core-in-shell concept is particularly advantageous for supporting any reactive sorbent which may lack the necessary strength to withstand extensive physical handling or repeated changes in specific volume as it is loaded and regenerated.
  • the shell itself can be made of various refractory materials which do not react with the gases being treated.
  • Other potential shell materials include calcium aluminate cement, aluminum oxide, and various aluminates and silicates or various types of clay which are widely used for making ceramic and refractory products.
  • One of ordinary skill in the art would be able to ascertain additional core or shell materials appropriate to their particular application.
  • a small amount of a pore-forming component such as dry potato starch, can be mixed with the shell-forming material before being applied.
  • the starch, or other pore-forming component will decompose when the pellets are heated to a high temperature, thereby increasing the porosity of the shell.
  • An example of an alternative pore-forming component is granular polyethylene glycol. Any material known to one of ordinary skill in the art which will form pores (i.e. decompose at high temperature/temperature of use) without interfering with the purposes of this invention can be used.
  • An alternative pore-forming material is limestone itself which can be incorporated in the shell because heating the pellets to the temperature of use will decompose the limestone in the shell and provide sufficient porosity.
  • Appropriate catalysts for use in the invention include any catalyst for the steam reforming of hydrocarbons.
  • the catalyst may also be one used for the water gas shift reaction.
  • These two types of catalysts are well known in the art and may include one or more of the following metals and/or oxides of the same: tungsten, cobalt, molybdenum, vanadium, potassium, lanthanum, iron, platinum, palladium, ruthenium, zinc, chromium, copper, or nickel.
  • cobalt and molybdenum are the preferred catalysts since, unlike nickel, they tend to withstand inactivation in the presence of large amounts of sulfur compounds in the feed gas. If the feed gas is relatively pure, nickel is the preferred catalyst.
  • a reforming catalyst can be prepared by impregnating a porous shell with any of the metals listed above in salt form, such as oxide.
  • the catalyst/sorbents of this invention can be produced by any method which provides the desired physical and chemical characteristics, one of the preferred methods is as follows.
  • the pellet cores are prepared by placing a measured amount of one or more powdered core-forming materials in a revolving drum or inclined pan pelletizer. While in the pelletizer, the powder is moistened with a water spray that causes the core material to ball up into small pellets. The conditions can be controlled to produce pellets of a desired diameter.
  • the pellets are sized by screening and those of an appropriate size are coated in the next step with the shell-forming material.
  • the powdered material for the protective layer e.g., cement or alumina
  • the pelletizing drum or inclined pan pelletizer while the pellets are being sprayed at set intervals with water.
  • dilute lignin solution may be included as a temporary binder in the coating process.
  • the process can be carried out continuously by using two pelletizing drums in series separated by a vibrating screen.
  • the core forming ingredients are supplied at a constant and controlled rate to the first pelletizing drum, and as the spherical cores are formed, they are discharged onto the vibrating screen.
  • the material which passes through the screen is returned to the first pelletizing drum for repelletizing.
  • the pellets that do not pass through the screen are conducted to the second pelletizing drum for coating with the shell-forming material.
  • the pellets are preferably comprised of cores ranging from about 3-8 mm in diameter and of shells ranging from about 0.3-1.0 mm in thickness.
  • Pellets prepared for commercial application can be either smaller or larger.
  • One of skill in the art would be able to choose the core and shell dimensions that will work best for the particular application of interest.
  • pellets coated with hydraulic cement are optionally cured in a steam atmosphere at 100° C. for about 1-3 days. In the case of alumina-coated pellets, neither air drying nor steam curing is required.
  • the pellets are calcined in air at about 1100° C. for 2 hr., causing partial sintering of the shell material to produce a strong but porous structure. Calcination also alters the core material by decomposing CaCO 3 in the case of limestone cores or removing water of crystallization in the case of plaster of Paris cores. However, the calcium sulfate present in plaster cores is left largely intact.
  • the pellets are treated at 1050° to 1100° C. to several cycles of reduction and oxidation.
  • the pellets are treated with a reducing gas, e.g. 10% H 2 or 30% CO in nitrogen, for 1 to 3 minutes, and during the oxidizing phase the pellets are treated with an oxidizing gas, e.g. air, for 1 to 3 minutes.
  • a reducing gas e.g. 10% H 2 or 30% CO in nitrogen
  • an oxidizing gas e.g. air
  • One method is the pore volume impregnation technique which is used to fill the shell pores with a saturated solution of the metal catalyst in salt form.
  • the pellets are contacted with sufficient solution only to the extent necessary to saturate the porous shell.
  • the pellets are then dried to remove the water and to deposit the metal catalyst within the pores. This impregnation process may be repeated until the desired level of impregnation is achieved.
  • the pellets are next heated to a temperature ranging from about 300°-700° C., with a temperature of about 500° C. being preferred, in order to decompose the metal salt, thereby converting it to the oxide form.
  • the catalyst is subsequently activated by an appropriate treatment. In the case of a nickel catalyst, the pellets are treated with hydrogen at about 300-500° C. to reduce the nickel oxide to its elemental metal form.
  • the pellets are treated with carbon dioxide gas at 500-800° C. to convert the CaO cores to CaCO 3 cores.
  • the pellets are then cooled to ambient temperature and the pore volume impregnation technique is used to fill the shell pores with an aqueous solution of metal salt.
  • the pellets are subsequently dried to remove the water and to deposit the metal salt with the pores of the pellet. Again, multiple impregnations may be used to achieve the requisite amount of loading of the metal catalyst.
  • the pellets are then heated to decompose the metal salt and thereafter treated to activate the catalyst in the manner outlined above.
  • Reaction (1) illustrates the reaction of methane with steam to produce carbon dioxide and hydrogen, and preferably employs a Ni catalyst.
  • Reaction (2) illustrates the reaction of CO with steam to produce CO 2 and H 2 which is known as the water gas shift reaction. This reaction preferably uses an iron oxide catalyst.
  • An alcohol solution of nickel salt is prepared by dissolving either nickel acetate, Ni(C 2 H 3 O 2 ).4H 2 O, or nickel nitrate, Ni(NO 3 ) 2 .6H 2 O, in 95% ethanol (5% water) to form a saturated solution of the salt.
  • Core-in-shell pellets are contacted with a limited quantity of solution, then dried to remove the solvent and to leave the salt behind in the pores. The process of impregnation can be repeated several times to achieve the desired nickel loading in the pellets.
  • the pellets are then heated to 500° C. to decompose the nickel salt and thereby convert it into nickel oxide.
  • the pellets are subsequently treated with hydrogen at 300-500° C. to reduce the nickel oxide to nickel.
  • the pellets Prior to impregnating the core-in-shell pellets with catalyst, the pellets are treated with carbon dioxide gas at 500 to 800° C. to convert the CaO cores to CaCO 3 cores.
  • the pellets are cooled to ambient temperature and the pore volume impregnation technique described in Example 1 is used to fill the shell pores with an aqueous solution of a nickel salt.
  • a solution containing 10-30 wt. % Ni(NO 3 ) 2 is suitable for this purpose.
  • the pellets are subsequently dried to remove the water and to deposit the nickel salt within the pore. Multiple impregnations can be used to achieve the desired nickel loading.
  • the pellets are then heated to 500° C. to decompose the nickel salt and further heated to 900° C. to convert CaCO 3 in the core material to CaO.
  • the pellets are subsequently treated with hydrogen at 300-500° C. to reduce the nickel oxide to nickel.
  • compositions and methods of this invention may be extended to other chemical reaction systems which require a solid catalyst and where it is advantageous to separate the products of reaction by selective absorption of a reaction product. Also, modifications of the composition and the ranges expressed herein may be made and still come within the scope and spirit of the present invention.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
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Abstract

A catalyst and sorbent is disclosed which comprises pellets with an absorbent core and a protective shell with a catalyst in the shell. Such material is especially well suited for steam reforming of hydrocarbons to produce hydrogen since a reforming catalyst can be incorporated in the shell and a sorbent for the by-product carbon dioxide can be used for the core. It is also well suited for producing hydrogen from carbon monoxide by means of the water gas shift reaction. The shell can be made sufficiently strong and durable for moving bed applications as well as fixed bed applications.

Description

    PRIORITY CLAIM
  • This application is a Divisional of U.S. patent application Ser. No. 10/218,803 filed Aug. 14, 2002, which application claims priority to U.S. Provisional Application Ser. No. 60/312,529 filed Aug. 15, 2001 and is incorporated by reference in its entirety.
    • FIELD OF THE INVENTION
  • This invention relates to a pelletized material having an absorbent core encased in a strong but porous shell having catalytic properties. Such a material is preferred for industrial chemical processes which produce hydrogen and carbon dioxide. These processes include the steam reforming of hydrocarbons and processes based on the water gas shift reaction.
    • BACKGROUND OF THE INVENTION
  • Hydrogen is an important raw material in the chemical and petroleum industries. Large quantities are used in the manufacture of ammonia and methanol and in a variety of petroleum hydrotreating processes.
  • Making hydrogen from methane is of particular interest because in the future hydrogen will be used for the generation of electric power by employing highly efficient fuel cells. While methane is the principal component of natural gas and may be plentiful, it can also be produced by hydrogasification of coal.
  • Currently, the primary method for converting methane and other light hydrocarbons to produce hydrogen is based on steam reforming. The steam methane reforming (SMR) process often involves multiple steps and severe operating conditions, including high temperatures and pressures.
  • A proposed method for improving the efficiency of steam methane reforming (SMR) is the Sorption Enhanced Reaction Process (SERP). The SERP method uses a fixed packed bed of an admixture of an SMR catalyst and a chemisorbent to remove carbon dioxide selectively from the reaction zone. The SERP process allows for the use of lower temperatures then those utilized in conventional SMR methods, and provides a higher degree of purity of the resulting hydrogen product.
  • Within the last few years, the concept of combining reaction and separation steps to simplify various chemical processes, conserve energy, and/or to improve product quality and yield has become economically attractive. Reactive distillation is one method that has been recently commercialized, along with membrane reactors. Membrane-based reaction systems may involve the use of metallic membranes which only small molecules like hydrogen can permeate, or polymeric, ceramic, and zeolitic membranes. The membranes may act as permselective barriers, or as an integral part of the catalytically active surface.
  • The present inventors have now discovered a unique method of producing hydrogen through the reaction of steam with methane, other light hydrocarbons, or carbon monoxide using a catalyst and sorbent combined in the same pelletized material. The method is unique compared to presently available technology in that it does not require the catalytic reforming and product separation steps to be conducted with different materials in completely separate steps.
  • It is therefore a primary objective of the claimed invention to provide a material that is capable of converting methane, other light hydrocarbons, or carbon monoxide to hydrogen and at the same time separate the hydrogen from carbon dioxide co-product.
  • It is a further objective of the present invention to provide a one-step method of producing hydrogen through the conversion of methane, other light hydrocarbons, or carbon monoxide using a singular material.
  • It is a further objective of the present invention to provide a material that is regenerable.
  • It is a further objective of the present invention to provide a material that includes a catalyst to enhance and promote the conversion of methane to hydrogen.
  • It is yet a further objective of the present invention to provide a material that is durable and attrition resistant.
  • It is still a further objective of the present invention to provide a material that is economical to manufacture and use.
  • These and other objectives will become apparent after review of the following description and claims of the invention which follow.
    • SUMMARY OF THE INVENTION
  • The invention describes a catalyst and sorbent in pellet form wherein each pellet combines a reactive core with a porous protective shell having a catalyst embedded or coated on the surface of the pores of the shell. Such materials are useful for various hydrogen manufacturing processes, and specifically for catalytically reforming methane or other hydrocarbon gases to produce hydrogen and carbon dioxide while at the same time separating the hydrogen from the carbon dioxide.
    • DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
  • The core-in-shell catalyst and sorbent of this invention includes a core of reactive, but comparatively physically weak, material and a strong but porous shell with catalytic properties. The shell maintains the structural integrity of the catalyst and sorbent during its use. The sorbent is also preferably able to retain its structural integrity during numerous cycles of use and regeneration.
  • The core is made of any material which will absorb or react with carbon dioxide (CO2) in order to remove it from the H2-containing product. The shell of the sorbent is a material which gives the pellet sufficient strength while allowing CO2 gas to penetrate to (diffuse to) the sorbent material in the core. With a calcium oxide core, the successful protective layer (shell) can be largely refractory cement or alumina. Preferred materials for the preparation of CaO cores include powdered limestone, dolomite, and plaster of Paris.
  • Types I, III, and IV Portland cement, high alumina cement (HAC), and calcium aluminate refractory cement can be used as shell materials. These are hydraulic cements which require curing. An alternative shell material is comprised of a sinterable powder (e.g., alumina) which upon heat treatment forms a strong, porous shell. Examples of core and shell raw materials which are appropriate for use in this invention include, but are not limited to, the following:
    Core material: Shell material:
    CaO (lime & swollen lime) Bentonite clay
    CaCO3 (limestone, swollen Attapulgite clay
    limestone)
    CaCO3•MgCO3 (dolomite) Zeolite material
    MgO Portland cements
    SrO High temperature refractory cement
    BaO Alumina
    Fly ash
    Calcium aluminates
    Magnesium oxysulfate cement
  • It may also be possible to use CaO.MgO derived from dolomite as a core material for removing CO2 from gas produced by gasifying coal. In this respect, it is believed the following reaction takes place:
    CaO.MgO(s)+CO2(g)
    Figure US20070129243A1-20070607-P00900
    CaCO3.MgO(s)
  • While MgO does not participate in the reaction, it serves to maintain the structural integrity and chemical reactivity of the sorbent.
  • The core-in-shell concept is not limited to the specifically-listed materials above. The concept can be applied to other absorbent materials which lack the necessary strength and durability in themselves to withstand repeated loading and regeneration. The effects of loading and regeneration can be particularly severe where the sorbent is converted from one chemical species to another during loading and then is converted back to the original species during regeneration. Such changes are accompanied by changes in the physical structure of the material which can produce changes in the specific volume of the material. Repeated swelling and shrinking of the material as it is loaded and regenerated can weaken the material and lead to spalling and disintegration. This type of failure has been observed with zinc-based sorbents for H2S where the material undergoes significant changes in specific volume during regeneration.
  • The core-in-shell concept is particularly advantageous for supporting any reactive sorbent which may lack the necessary strength to withstand extensive physical handling or repeated changes in specific volume as it is loaded and regenerated. The shell itself can be made of various refractory materials which do not react with the gases being treated. Other potential shell materials include calcium aluminate cement, aluminum oxide, and various aluminates and silicates or various types of clay which are widely used for making ceramic and refractory products. One of ordinary skill in the art would be able to ascertain additional core or shell materials appropriate to their particular application.
  • A small amount of a pore-forming component, such as dry potato starch, can be mixed with the shell-forming material before being applied. The starch, or other pore-forming component, will decompose when the pellets are heated to a high temperature, thereby increasing the porosity of the shell. An example of an alternative pore-forming component is granular polyethylene glycol. Any material known to one of ordinary skill in the art which will form pores (i.e. decompose at high temperature/temperature of use) without interfering with the purposes of this invention can be used.
  • An alternative pore-forming material is limestone itself which can be incorporated in the shell because heating the pellets to the temperature of use will decompose the limestone in the shell and provide sufficient porosity.
  • Although increasing shell thickness can increase pellet strength, it can also reduce the rate of diffusion through the shell and reduce sorbent capacity. One of ordinary skill in the art can optimize the composition for adsorption capacity versus crushing strength for a desired application.
  • Appropriate catalysts for use in the invention include any catalyst for the steam reforming of hydrocarbons. The catalyst may also be one used for the water gas shift reaction. These two types of catalysts are well known in the art and may include one or more of the following metals and/or oxides of the same: tungsten, cobalt, molybdenum, vanadium, potassium, lanthanum, iron, platinum, palladium, ruthenium, zinc, chromium, copper, or nickel. When catalytically reforming methane in the presence of a sulfide impurity (for e.g., H2S), it is believed that cobalt and molybdenum are the preferred catalysts since, unlike nickel, they tend to withstand inactivation in the presence of large amounts of sulfur compounds in the feed gas. If the feed gas is relatively pure, nickel is the preferred catalyst.
  • While various methods can be used for incorporating a catalyst-forming material in the shell, one method is to mix such a material with the other shell-forming materials before they are applied. Another method is to impregnate core-in-shell pellets with the catalyst after the pellets have been made. For example, a reforming catalyst can be prepared by impregnating a porous shell with any of the metals listed above in salt form, such as oxide.
  • Although the catalyst/sorbents of this invention can be produced by any method which provides the desired physical and chemical characteristics, one of the preferred methods is as follows. The pellet cores are prepared by placing a measured amount of one or more powdered core-forming materials in a revolving drum or inclined pan pelletizer. While in the pelletizer, the powder is moistened with a water spray that causes the core material to ball up into small pellets. The conditions can be controlled to produce pellets of a desired diameter. The pellets are sized by screening and those of an appropriate size are coated in the next step with the shell-forming material.
  • In coating the pellet cores with the protective layer, the powdered material for the protective layer, e.g., cement or alumina, is added to the pelletizing drum or inclined pan pelletizer while the pellets are being sprayed at set intervals with water. In some cases, dilute lignin solution may be included as a temporary binder in the coating process. The process can be carried out continuously by using two pelletizing drums in series separated by a vibrating screen. The core forming ingredients are supplied at a constant and controlled rate to the first pelletizing drum, and as the spherical cores are formed, they are discharged onto the vibrating screen. The material which passes through the screen is returned to the first pelletizing drum for repelletizing. The pellets that do not pass through the screen are conducted to the second pelletizing drum for coating with the shell-forming material.
  • The pellets are preferably comprised of cores ranging from about 3-8 mm in diameter and of shells ranging from about 0.3-1.0 mm in thickness. Pellets prepared for commercial application can be either smaller or larger. One of skill in the art would be able to choose the core and shell dimensions that will work best for the particular application of interest.
  • Once coated, the pellets are dried and screened to provide pellets of a uniform and appropriate size. Pellets coated with hydraulic cement are optionally cured in a steam atmosphere at 100° C. for about 1-3 days. In the case of alumina-coated pellets, neither air drying nor steam curing is required. The pellets are calcined in air at about 1100° C. for 2 hr., causing partial sintering of the shell material to produce a strong but porous structure. Calcination also alters the core material by decomposing CaCO3 in the case of limestone cores or removing water of crystallization in the case of plaster of Paris cores. However, the calcium sulfate present in plaster cores is left largely intact.
  • In order to convert CaSO4 plaster of Paris cores to CaO, the pellets are treated at 1050° to 1100° C. to several cycles of reduction and oxidation. During the reducing phase of each cycle, the pellets are treated with a reducing gas, e.g. 10% H2 or 30% CO in nitrogen, for 1 to 3 minutes, and during the oxidizing phase the pellets are treated with an oxidizing gas, e.g. air, for 1 to 3 minutes.
  • There are several different appropriate methods that may be used to incorporate the shell material with a reforming catalyst depending on the catalytic material selected. One method is the pore volume impregnation technique which is used to fill the shell pores with a saturated solution of the metal catalyst in salt form. The pellets are contacted with sufficient solution only to the extent necessary to saturate the porous shell. The pellets are then dried to remove the water and to deposit the metal catalyst within the pores. This impregnation process may be repeated until the desired level of impregnation is achieved. The pellets are next heated to a temperature ranging from about 300°-700° C., with a temperature of about 500° C. being preferred, in order to decompose the metal salt, thereby converting it to the oxide form. The catalyst is subsequently activated by an appropriate treatment. In the case of a nickel catalyst, the pellets are treated with hydrogen at about 300-500° C. to reduce the nickel oxide to its elemental metal form.
  • In a second method, prior to the impregnation method described above, the pellets are treated with carbon dioxide gas at 500-800° C. to convert the CaO cores to CaCO3 cores. The pellets are then cooled to ambient temperature and the pore volume impregnation technique is used to fill the shell pores with an aqueous solution of metal salt. The pellets are subsequently dried to remove the water and to deposit the metal salt with the pores of the pellet. Again, multiple impregnations may be used to achieve the requisite amount of loading of the metal catalyst. The pellets are then heated to decompose the metal salt and thereafter treated to activate the catalyst in the manner outlined above.
  • The hydrogen production process of this invention can employ either of the two types of primary chemical reactions, shown below:
    CH4(g)+2H2O(g)=CO2(g)+4H2(g)  (1)
    CO(g)+H2O(g)=CO2(g)+H2(g)  (2)
  • Reaction (1) illustrates the reaction of methane with steam to produce carbon dioxide and hydrogen, and preferably employs a Ni catalyst. Reaction (2) illustrates the reaction of CO with steam to produce CO2 and H2 which is known as the water gas shift reaction. This reaction preferably uses an iron oxide catalyst. The sorbent of the invention removes carbon dioxide (CO2) from the hot gas stream by means of the following reaction (using CaO as an example):
    CaO(s)+CO2(g)=CaCO3(s)  (3)
  • The combination of an absorbent core and a catalytic shell offers at least two important advantages over prior art processes. First, the presence of a strong absorbent for the carbon dioxide helps to drive either reaction (1) or (2) which can be limited by thermodynamic equilibrium. Second, the heat absorbed by the highly endothermic reactions (1) and (2) is largely offset by the heat generated by reaction (3). Therefore, there is little need to either add or remove heat from the reaction as a whole, which greatly simplifies the design of the reaction system and improves the overall efficiency and economics of the process.
  • The following examples are offered to illustrate but not limit the invention. Thus, they are presented with the understanding that various formulation modifications as well as method of delivery modifications may be made and still be within the spirit of the invention.
    • EXAMPLE 1
  • Pore Volume Impregnation Technique Using Nickel
  • An alcohol solution of nickel salt is prepared by dissolving either nickel acetate, Ni(C2H3O2).4H2O, or nickel nitrate, Ni(NO3)2.6H2O, in 95% ethanol (5% water) to form a saturated solution of the salt. Core-in-shell pellets are contacted with a limited quantity of solution, then dried to remove the solvent and to leave the salt behind in the pores. The process of impregnation can be repeated several times to achieve the desired nickel loading in the pellets. The pellets are then heated to 500° C. to decompose the nickel salt and thereby convert it into nickel oxide. The pellets are subsequently treated with hydrogen at 300-500° C. to reduce the nickel oxide to nickel.
    • EXAMPLE 2
  • Pore Volume Impregnation Technique Using Nickel and CaO Pellet Cores With Carbon Dioxide Pretreatment
  • Prior to impregnating the core-in-shell pellets with catalyst, the pellets are treated with carbon dioxide gas at 500 to 800° C. to convert the CaO cores to CaCO3 cores. The pellets are cooled to ambient temperature and the pore volume impregnation technique described in Example 1 is used to fill the shell pores with an aqueous solution of a nickel salt. A solution containing 10-30 wt. % Ni(NO3)2 is suitable for this purpose. The pellets are subsequently dried to remove the water and to deposit the nickel salt within the pore. Multiple impregnations can be used to achieve the desired nickel loading. The pellets are then heated to 500° C. to decompose the nickel salt and further heated to 900° C. to convert CaCO3 in the core material to CaO. The pellets are subsequently treated with hydrogen at 300-500° C. to reduce the nickel oxide to nickel.
  • It should be appreciated that the compositions and methods of this invention may be extended to other chemical reaction systems which require a solid catalyst and where it is advantageous to separate the products of reaction by selective absorption of a reaction product. Also, modifications of the composition and the ranges expressed herein may be made and still come within the scope and spirit of the present invention.
  • Having described the invention with reference to particular compositions, theories of effectiveness, and the like, it will be apparent to those of skill in the art that it is not intended that the invention be limited by such illustrative embodiments or mechanisms, and that modifications can be made without departing from the scope or spirit of the invention, as defined by the appended claims. It is intended that all such obvious modifications and variations be included within the scope of the present invention as defined in the appended claims. The claims are meant to cover the claimed components and steps in any sequence which is effective to meet the objectives there intended, unless the context specifically indicates to the contrary.
  • All articles cited herein and in the following list are hereby expressly incorporated in their entirety by reference.
    • CITATIONS
    • Akiti, Jr., T. T., et al. A regenerable calcium-based core-in-shell sorbent for desulfurizing hot coal gas. Ind. Eng. Chem. Res. 2002, 41, 587-597.
    • Balasubramanian, B. et al. Hydrogen from methane in a single-step process. Chem. Eng. Sci. 1999, 54, 3543-3552.
    • Ding, Y. et al. Adsorption-enhanced steam-methane reforming. Chem. Eng. Sci. 2000, 55, 3929-3940.
    • Hufton, J. R. et al. Sorption-enhanced reaction process for hydrogen production. AIChE J., 1999, 45, 248-256.

Claims (8)

1. A method of manufacturing a composition for producing hydrogen from industrial gas-phase chemical reactions comprising: forming an interior core that reacts with or absorbs CO2; coating the core with a protective shell; and incorporating a catalyst into the protective shell.
2. The method of claim 1 wherein the interior core is formed by pelletizing a core-forming material selected from the group consisting of limestone, lime, dolomite, plaster of Paris, anhydrite, and gypsum.
3. The method of claim 2 further including the step of drying and screening the core-forming material to form pellets of a uniform size following the coating step.
4. The method of claim 1 whereby the shell is comprised of hydraulic cement, and the method further includes the step of curing the core following the coating step in a steam atmosphere at 100° C. for about 1-3 days.
5. The method of claim 1 whereby the shell is comprised of a material selected from the group consisting of alumina, limestone, and plaster of Paris, and the method further includes the step of calcining the core following the coating step to cause partial sintering of the shell material.
6. The method of claim 1 whereby the catalyst is incorporated into the shell by impregnating the shell with a solution of the catalyst.
7. The method of claim 6 whereby the impregnation step is repeated at least once.
8. The method of claim 1 whereby the core is treated with carbon dioxide at 500-800° C. following the coating step and prior to the catalyst incorporation step.
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US20080193370A1 (en) * 2003-11-26 2008-08-14 Cabot Corporation Fuel reformer catalyst and absorbent materials
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WO2013003948A1 (en) * 2011-07-04 2013-01-10 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources Sorbent pellets including oxygen carriers
US8362278B2 (en) 2010-10-01 2013-01-29 Chevron Phillips Chemical Company Lp Methods for the conversion of a substituted furan to a substituted pyrrole

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DE10313702A1 (en) * 2003-03-27 2004-10-07 Basf Ag Catalyst and process for the hydrogenation of carbonyl compounds
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Citations (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4316813A (en) * 1980-08-04 1982-02-23 Engelhard Minerals & Chemicals Corp. Limestone-based sorbent agglomerates for removal of sulfur compounds in hot gases and method of making
US4548912A (en) * 1980-04-14 1985-10-22 Ashland Oil, Inc. Microspherical catalysts
US4701436A (en) * 1984-04-23 1987-10-20 California Institute Of Technology Catalytic, hollow, refractory spheres
US4916171A (en) * 1984-07-25 1990-04-10 Rohm And Haas Company Polymers comprising alkali-insoluble core/alkali-soluble shell and copositions thereof
US5077253A (en) * 1987-12-28 1991-12-31 Mobil Oil Corporation Layered cracking catalyst and method of manufacture and use thereof
US5082814A (en) * 1991-01-31 1992-01-21 Engelhard Corporation Shell-coated FCC catalysts
US5179054A (en) * 1987-12-28 1993-01-12 Mobil Oil Corporation Layered cracking catalyst and method of manufacture and use thereof
US5221656A (en) * 1992-03-25 1993-06-22 Amoco Corporation Hydroprocessing catalyst
US5228980A (en) * 1991-01-31 1993-07-20 Engelhard Corporation Fluidized catalytic cracking process employing shell-coated FCC catalysts
US5286370A (en) * 1987-12-28 1994-02-15 Mobil Oil Corporation Catalytic cracking using a layered cracking catalyst
US5433939A (en) * 1994-03-14 1995-07-18 Wheelock; Thomas D. Cyclic process for oxidation of calcium sulfide
US5653955A (en) * 1994-03-14 1997-08-05 Iowa State University Research Foundation Inc. Cyclic process for oxidation of calcium sulfide
US5703003A (en) * 1994-03-23 1997-12-30 United States Department Of Energy Durable regenerable sorbent pellets for removal of hydrogen sulfide from coal gas
US5774779A (en) * 1996-11-06 1998-06-30 Materials And Electrochemical Research (Mer) Corporation Multi-channel structures and processes for making such structures
US5935889A (en) * 1996-10-04 1999-08-10 Abb Lummus Global Inc. Catalyst and method of preparation
US6476147B1 (en) * 1993-06-01 2002-11-05 Spalding Sports Worldwide, Inc. Multi-layer golf ball utilizing silicone materials
US6528683B1 (en) * 1998-06-03 2003-03-04 Basf Aktiengesellschaft Method for producing shell catalysts for the catalytic vapor-phase oxidation of aromatic hydrocarbons and catalysts obtained in such a manner
US6582819B2 (en) * 1998-07-22 2003-06-24 Borden Chemical, Inc. Low density composite proppant, filtration media, gravel packing media, and sports field media, and methods for making and using same
US6586361B1 (en) * 1998-08-27 2003-07-01 Basf Aktiengesellschaft Multilayered shell catalysts for catalytic gaseous phase oxidation of aromatic hydrocarbons
US6890592B2 (en) * 2002-03-13 2005-05-10 Appleton Papers Inc. Uniform microcapsules

Patent Citations (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4548912A (en) * 1980-04-14 1985-10-22 Ashland Oil, Inc. Microspherical catalysts
US4316813A (en) * 1980-08-04 1982-02-23 Engelhard Minerals & Chemicals Corp. Limestone-based sorbent agglomerates for removal of sulfur compounds in hot gases and method of making
US4701436A (en) * 1984-04-23 1987-10-20 California Institute Of Technology Catalytic, hollow, refractory spheres
US4916171A (en) * 1984-07-25 1990-04-10 Rohm And Haas Company Polymers comprising alkali-insoluble core/alkali-soluble shell and copositions thereof
US5077253A (en) * 1987-12-28 1991-12-31 Mobil Oil Corporation Layered cracking catalyst and method of manufacture and use thereof
US5179054A (en) * 1987-12-28 1993-01-12 Mobil Oil Corporation Layered cracking catalyst and method of manufacture and use thereof
US5286370A (en) * 1987-12-28 1994-02-15 Mobil Oil Corporation Catalytic cracking using a layered cracking catalyst
US5082814A (en) * 1991-01-31 1992-01-21 Engelhard Corporation Shell-coated FCC catalysts
US5228980A (en) * 1991-01-31 1993-07-20 Engelhard Corporation Fluidized catalytic cracking process employing shell-coated FCC catalysts
US5221656A (en) * 1992-03-25 1993-06-22 Amoco Corporation Hydroprocessing catalyst
US6476147B1 (en) * 1993-06-01 2002-11-05 Spalding Sports Worldwide, Inc. Multi-layer golf ball utilizing silicone materials
US5653955A (en) * 1994-03-14 1997-08-05 Iowa State University Research Foundation Inc. Cyclic process for oxidation of calcium sulfide
US5433939A (en) * 1994-03-14 1995-07-18 Wheelock; Thomas D. Cyclic process for oxidation of calcium sulfide
US5703003A (en) * 1994-03-23 1997-12-30 United States Department Of Energy Durable regenerable sorbent pellets for removal of hydrogen sulfide from coal gas
US5935889A (en) * 1996-10-04 1999-08-10 Abb Lummus Global Inc. Catalyst and method of preparation
US5774779A (en) * 1996-11-06 1998-06-30 Materials And Electrochemical Research (Mer) Corporation Multi-channel structures and processes for making such structures
US6528683B1 (en) * 1998-06-03 2003-03-04 Basf Aktiengesellschaft Method for producing shell catalysts for the catalytic vapor-phase oxidation of aromatic hydrocarbons and catalysts obtained in such a manner
US6582819B2 (en) * 1998-07-22 2003-06-24 Borden Chemical, Inc. Low density composite proppant, filtration media, gravel packing media, and sports field media, and methods for making and using same
US6586361B1 (en) * 1998-08-27 2003-07-01 Basf Aktiengesellschaft Multilayered shell catalysts for catalytic gaseous phase oxidation of aromatic hydrocarbons
US6890592B2 (en) * 2002-03-13 2005-05-10 Appleton Papers Inc. Uniform microcapsules

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20080193370A1 (en) * 2003-11-26 2008-08-14 Cabot Corporation Fuel reformer catalyst and absorbent materials
US7578986B2 (en) * 2003-11-26 2009-08-25 Cabot Corporation Fuel reformer catalyst and absorbent materials
US20100081567A1 (en) * 2008-09-29 2010-04-01 Sud-Chemie Inc. Process for sulfiding catalysts for a sour gas shift process
US8846564B2 (en) * 2008-09-29 2014-09-30 Clariant Corporation Process for sulfiding catalysts for a sour gas shift process
US8362278B2 (en) 2010-10-01 2013-01-29 Chevron Phillips Chemical Company Lp Methods for the conversion of a substituted furan to a substituted pyrrole
WO2013003948A1 (en) * 2011-07-04 2013-01-10 Her Majesty The Queen In Right Of Canada As Represented By The Minister Of Natural Resources Sorbent pellets including oxygen carriers

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