+

WO2009111335A2 - Compositions de charbon pour gazéification catalytique - Google Patents

Compositions de charbon pour gazéification catalytique Download PDF

Info

Publication number
WO2009111335A2
WO2009111335A2 PCT/US2009/035557 US2009035557W WO2009111335A2 WO 2009111335 A2 WO2009111335 A2 WO 2009111335A2 US 2009035557 W US2009035557 W US 2009035557W WO 2009111335 A2 WO2009111335 A2 WO 2009111335A2
Authority
WO
WIPO (PCT)
Prior art keywords
particulate
wet cake
coal
slurry
petroleum coke
Prior art date
Application number
PCT/US2009/035557
Other languages
English (en)
Other versions
WO2009111335A3 (fr
Inventor
Alkis S. Rappas
George Frederick Salem
Original Assignee
Greatpoint Energy, Inc.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Greatpoint Energy, Inc. filed Critical Greatpoint Energy, Inc.
Publication of WO2009111335A2 publication Critical patent/WO2009111335A2/fr
Publication of WO2009111335A3 publication Critical patent/WO2009111335A3/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0943—Coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1656—Conversion of synthesis gas to chemicals
    • C10J2300/1662—Conversion of synthesis gas to chemicals to methane
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam only

Definitions

  • the invention relates to particulate compositions of coal and petroleum coke, and at least one alkali metal gasification catalyst, one transition metal gasification catalyst, and one alkaline earth metal source. Further, the invention relates to processes for preparation of the particulate compositions and for gasification of the same in the presence of steam to form gaseous products, and in particular, methane.
  • Petroleum coke is a generally solid carbonaceous residue derived from the delayed coking or fluid coking a carbon source such as a crude oil residue, and the coking processes used for upgrading oil sand.
  • Petroleum cokes in general, have poor gasification reactivity, particularly at moderate temperatures, due to their highly crystalline carbon and elevated levels of organic sulfur derived from heavy-gravity oil.
  • Use of catalysts is necessary for improving the lower reactivity of petroleum cokes, however, certain types of catalysts can be poisoned by the sulfur-containing compounds in the petcokes.
  • the invention provides a particulate composition comprising an intimate mixture, the intimate mixture comprising:
  • transition gasification catalyst, the alkaline earth metal source, and alkali metal gasification catalyst are loaded onto the coal particulate, the petroleum coke particulate, or both;
  • the particulate composition in the presence of steam and under suitable temperature and pressure, the particulate composition exhibits gasification activity whereby a plurality of gases including methane and at least one or more of hydrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, ammonia, and other higher hydrocarbons are formed;
  • the transition metal gasification catalyst is present in an amount sufficient to provide, in the particulate composition, a ratio of transition metal atoms to carbon atoms ranging from about 0.001 to about 0.10;
  • the alkaline earth metal source is present in an amount sufficient to provide, in the particulate composition, from about 0.1 wt% to about 3.0 wt% alkaline earth metal atoms on a dry basis;
  • the alkali metal gasification catalyst is present in an amount sufficient to provide, in the particulate composition, a ratio of alkali metal atoms to carbon atoms ranging from about 0.01 to about 0.08.
  • the invention provides a process for converting a particulate composition into a plurality of gaseous products, the process comprising the steps of: [0019] (a) supplying a particulate composition according to the first aspect of the invention to a gasification reactor;
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • step (d) contacting one of petroleum coke particulate, the first coal feedstock, the second coal feedstock or the third coal feedstock, other than the one used for step (c), with a second aqueous solution comprising an alkaline earth metal source to form a second slurry;
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • step (d) contacting one of petroleum coke particulate, the first coal feedstock or the second coal feedstock, other than the one used for step (c), with a second aqueous solution comprising an alkaline earth metal source to form a second slurry;
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • step (d) contacting one of petroleum coke particulate, the first coal feedstock, the second coal feedstock or the third coal feedstock, other than the one used for step (c), with a second aqueous solution comprising an alkaline earth metal source to form a second slurry;
  • step (c), (d) or (e) wherein, if the petroleum coke particulate is not used in step (c), (d) or (e), the third coal feedstock is provided and is used in one of steps (c), (d) or (e); and
  • the petroleum coke particulate is mixed with at least a portion of each of the first wet cake, the second wet cake and the third wet cake to form the final wet cake, which is optionally thermally treated with a dry inert gas as needed to form a particulate composition;
  • the petroleum coke particulate is mixed with at least a portion of the final wet cake, which is optionally thermally treated with a dry inert gas as needed to form a particulate composition; or
  • step (iii) the petroleum coke particulate is mixed with at least a portion of the particulate composition from step (h).
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • step (d) contacting one of petroleum coke particulate, the first coal feedstock or the second coal feedstock, other than the one used for step (c), with a second aqueous solution comprising an alkaline earth metal source to form a second slurry;
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a process for preparing a particulate composition, the process comprising the steps of:
  • the invention provides a particulate composition prepared according to the third through the fourteenth aspects of the invention.
  • the present invention relates to a particulate composition, methods for the preparation of the particulate composition, and methods for the catalytic gasification of the particulate composition.
  • the particulate composition includes one or more petroleum cokes in various blends with one or more coals, for example, high ash and/or high moisture content coals, particularly low ranking coals such as lignites, sub-bituminous coals, and mixtures thereof.
  • Such particulate compositions can provide for an economical and commercially practical process for catalytic gasification of coals, such as lignites or sub- bituminous coal, with high ash and moisture contents to yield methane and other value-added gases as a product.
  • Such particulate compositions also serve to reduce or eliminate some technical challenges associated with the catalytic gasification of petroleum coke.
  • the particulate compositions and processes described herein identify methods to efficiently exploit these different feeds in a commercially practical gasification process by processing them as blended feedstock.
  • the invention can be practiced, for example, using any of the developments to catalytic gasification technology disclosed in commonly owned US2007/0000177A1, US2007/0083072A1 and US2007/0277437A1; and U.S. Patent Application Serial Nos. 12/178,380 (filed 23 July 2008), 12/234,012 (filed 19 September 2008) and 12/234,018 (filed 19 September 2008). All of the above are incorporated by reference herein for all purposes as if fully set forth.
  • the terms “comprises,” “comprising,” “includes,” “including,” “has,” “having” or any other variation thereof, are intended to cover a non-exclusive inclusion.
  • a process, method, article, or apparatus that comprises a list of elements is not necessarily limited to only those elements but can include other elements not expressly listed or inherent to such process, method, article, or apparatus.
  • "or” refers to an inclusive or and not to an exclusive or. For example, a condition A or B is satisfied by any one of the following: A is true (or present) and B is false (or not present), A is false (or not present) and B is true (or present), and both A and B are true (or present).
  • petroleum coke includes both (i) the solid thermal decomposition product of high-boiling hydrocarbon fractions obtained in petroleum processing (heavy residues - "resid petcoke”); and (ii) the solid thermal decomposition product of processing tar sands (bituminous sands or oil sands - "tar sands petcoke”).
  • Such carbonization products include, for example, green, calcined, needle and fluidized bed petroleum coke.
  • Resid petcoke can be derived from a crude oil, for example, by coking processes used for upgrading heavy-gravity residual crude oil, which petroleum coke contains ash as a minor component, typically about 1.0 wt% or less, and more typically about 0.5 wt% of less, based on the weight of the coke.
  • the ash in such lower-ash cokes predominantly comprises metals such as nickel and vanadium.
  • Tar sands petcoke can be derived from an oil sand, for example, by coking processes used for upgrading oil sand.
  • Tar sands petcoke contains ash as a minor component, typically in the range of about 2 wt% to about 12 wt%, and more typically in the range of about 4 wt% to about 12 wt.%, based on the overall weight of the tar sands petcoke.
  • the ash in such higher-ash cokes predominantly comprises materials such as silica and/or alumina.
  • Petroleum coke in general has an inherently low moisture content typically in the range of from about 0.2 to about 2 wt% (based on total petroleum coke weight); it also typically has a very low water soaking capacity to allow for conventional catalyst impregnation methods.
  • the particulate composition of this invention eliminates this problem and uses the low moisture content in the petroleum coke for advantageous effects in a petroleum coke - coal blends.
  • the resulting particulate compositions contain, for example, a lower average moisture content which increases the efficiency of downstream drying operation versus conventional drying operations.
  • the petroleum coke can comprise at least about 70 wt% carbon, at least about 80 wt% carbon, or at least about 90 wt% carbon, based on the total weight of the petroleum coke.
  • the petroleum coke comprises less than about 20 wt% percent inorganic compounds, based on the weight of the petroleum coke.
  • coal as used herein means peat, lignite, sub-bituminous coal, bituminous coal, anthracite, or mixtures thereof.
  • the coal has a carbon content of less than about 90%, less than about 85%, or less than about 80%, or less than about 75%, or less than about 70%, or less than about 65%, or less than about 60%, or less than about 55%, or less than about 50% by weight, based on the total coal weight.
  • the coal has a carbon content ranging up to about 90%, or up to about 85%, or up to about 80%, or up to about 75% by weight, based on the total coal weight.
  • Examples of useful coals include, but are not limited to, Illinois #6, Pittsburgh #8, Beulah (ND), Utah Blind Canyon, and Powder River Basin (PRB) coals.
  • Anthracite, bituminous coal, sub-bituminous coal, and lignite coal may contain about 10 wt%, from about 5 to about 7 wt%, from about 4 to about 8 wt %, and from about 9 to about 11 wt%, ash by total weight of the coal on a dry basis, respectively.
  • the ash content of any particular coal source will depend on the rank and source of the coal, as is familiar to those skilled in the art.
  • Particulate compositions of the invention are based on the above-described petroleum coke and coal, and further comprise an amount of an alkali metal gasification catalyst, a transition metal gasification catalyst, and an alkaline earth metal source.
  • the alkali metal gasification catalyst can be an alkali metal and/or a compound containing alkali metal atoms.
  • the alkali metal gasification catalyst can comprise one or more alkali metal complexes (e.g., coordination complexes formed with one or more reactive functionalities on the surface or within the pores of the coal particulate, such as carboxylic acids and/or phenolic groups) formed with the coal and/or petroleum coke particulate.
  • the quantity of the alkali metal component in the composition is sufficient to provide, in the particulate composition, a ratio of alkali metal atoms to carbon atoms ranging from about 0.01, or from about 0.02, or from about 0.03, or from about 0.04, to about 0.06, or to about 0.07, or to about 0.08.
  • Suitable alkali metals include lithium, sodium, potassium, rubidium, cesium, and mixtures thereof. Particularly useful are potassium sources. Suitable alkali metal sources include alkali metal carbonates, bicarbonates, formates, oxalates, amides, hydroxides, acetates, or similar compounds.
  • the catalyst can comprise one or more of sodium carbonate, potassium carbonate, rubidium carbonate, lithium carbonate, cesium carbonate, sodium hydroxide, potassium hydroxide, rubidium hydroxide or cesium hydroxide, and particularly, one or more potassium complexes formed with the coal particulate, potassium carbonate, potassium bicarbonate, potassium hydroxide, or mixtures thereof.
  • the alkali metal gasification catalyst comprises one or more potassium complexes formed with coal particulate, carbonates, bicarbonates, hydroxides, or mixtures thereof.
  • the alkaline earth metal source can be an alkaline earth metal and/or a compound containing alkaline earth metal atoms.
  • Typical alkaline earth metal sources can include magnesium, calcium, and/or barium sources, such as, but not limited to, magnesium oxide, magnesium hydroxide, magnesium carbonate, magnesium sulfate, calcium oxide, calcium hydroxide, calcium carbonate, calcium sulfate, barium oxide, barium hydroxide, barium carbonate, barium sulfate, or mixtures thereof.
  • the alkaline earth source comprises a source of calcium; in certain other embodiments, the source of calcium is calcium hydroxide, calcium sulfate, or mixtures thereof.
  • the quantity of alkaline earth metal source in the composition is sufficient to provide from about 0.1 wt% to about 3.0 wt%, or to about 2.0 wt%, alkaline earth atoms by dry weight.
  • the transition metal gasification catalyst can be a transition metal and/or a compound containing transition metal atoms.
  • Typical transition metal gasification catalysts can include sources, such as, but not limited to, V, Cr, Mn, Fe, Co, Ni, Cu, Mo, or mixtures thereof.
  • transition metal gasification catalyst can comprise one or more transition metal complexes (e.g., coordination complexes formed with one or more reactive functionalities on the surface or within the pores of the coal and/or petroleum coke particulate, such as carboxylic acids and/or phenolic groups).
  • the transition metal gasification catalyst comprises an Fe source, Mn source, or mixtures thereof.
  • the transition metal gasification catalyst comprises one or more iron or manganese complexes formed with the coal particulate, FeO, Fe 2 O 3 , FeSO 4 , MnO, MnO 2 , MnSO 4 , or mixtures thereof.
  • the quantity of transition metal gasification catalyst in the composition is sufficient to provide a ratio of transition metal atoms to carbon atoms ranging from about 0.001 to about 0.10.
  • each of the petroleum coke and coal sources can be supplied as a fine particulate having an average particle size of from about 25 microns, or from about 45 microns, up to about 2500 microns, or up to about 500 microns.
  • the particulate composition can have an average particle size which enables incipient fluidization of the particulate composition at the gas velocity used in the fluid bed gasification reactor.
  • At least the coal particulate of the particulate composition comprises a gasification catalyst and optionally, a co-catalyst/catalyst additive as discussed previously.
  • the gasification catalyst can comprise a source of at least one alkali metal and is present in an amount sufficient to provide, in the particulate composition, a ratio of alkali metal atoms to carbon atoms ranging from about 0.01, or from about 0.02, or from about 0.03, or from about 0.04, to about 0.08, or to about 0.07, or to about 0.06.
  • the ratio of the petroleum coke particulate and coal particulate in the particulate composition can be selected based on technical considerations, processing economics, availability, and proximity of the coal and petroleum coke sources. The availability and proximity of the two sources for these blends affect the price of the feeds, and thus the overall production costs of the catalytic gasification process.
  • the petroleum coke and the coal can be blended in at about 5:95, about 10:90, about 15:85, about 20:80, about 25:75, about 30:70, about 35:65, about 40:60, about 45:55, about 50:50, about 55:45, about 60:40, about 65:35, about 70:20, about 75:25, about 80:20, about 85:15, about 90:10, or about 95:5 by weight on a wet or dry basis, depending on the processing conditions.
  • the petroleum coke and coal sources, as well as the ratio of the petroleum coke particulate to the coal particulate can be used to control other material characteristics of the feedstock blend.
  • coal and other carbonaceous material include significant quantities of inorganic mater including calcium, alumina and silica which form inorganic oxides ("ash") in the gasification reactor.
  • inorganic mater including calcium, alumina and silica which form inorganic oxides ("ash") in the gasification reactor.
  • potassium and other alkali metals can react with the alumina and silica in ash to form insoluble alkali aluminosilicates.
  • the alkali metal is substantially water-insoluble and inactive as a catalyst.
  • a solid purge of char i.e., solids composed of ash, unreacted carbonaceous material, and various alkali metal compounds (both water soluble and water insoluble) are routinely withdrawn.
  • the alkali metal is recovered from the char, and any unrecovered catalyst is generally compensated by a catalyst make-up stream.
  • the ash content of the particulate composition can be selected to be, for example, to be about 20 wt% or less, or about 15 wt% or less, or about 10 wt% or less, depending on ratio of the particulates and/or the starting ash in the coal source.
  • the resulting particulate composition can comprise an ash content ranging from about 5 wt%, or from about 10 wt%, to about 20 wt%, or to about 15 wt%, based on the weight of the particulate composition. In other embodiments, the ash content of the particulate composition can comprise less than about 20 wt%, or less than about 15 wt%, or less than about 10 wt%, or less than about 8 wt%, or less than about 6 wt% alumina, based on the weight of the ash.
  • the resulting particulate composition can comprise an ash content of less than about 20 wt%, based on the weight of the particulate composition where the ash content of the particulate composition comprises less than about 20 wt% alumina, or less than about 15 wt% alumina, based on the weight of the ash.
  • alumina can react with alkali source to yield an insoluble char comprising, for example, an alkali aluminate or aluminosilicate.
  • insoluble char can lead to decreased catalyst recovery (i.e., increased catalyst loss), and thus, require additional costs of make-up catalyst in the overall gasification process, as will be discussed later.
  • the resulting particulate composition can have a significantly higher % carbon, and thus btu/lb value and methane product per unit weight of the particulate composition.
  • the resulting particulate composition has a carbon content ranging from about 75 wt%, or from about 80 wt%, or from about 85 wt%, or from about 90 wt%, up to about 95 wt%, based on the combined weight of the coal and petcoke.
  • the coal particulate, the petroleum coke particulate, or both are treated to load the particulate with a transition metal gasification catalyst, an alkali metal gasification catalyst, and an alkaline earth metal source.
  • the particulate is treated in at least three separate processing steps in which separate feedstocks of coal and/or petcoke particulate are contacted with separate solutions (i.e., loading solutions). At least three separate loading solutions are used to load gasification catalyst or alkaline earth metal source onto separate feedstocks of carbonaceous particulate.
  • one loading solution is an aqueous solution comprising a transition metal gasification catalyst, another is an aqueous solution comprising an alkali metal gasification catalyst, and another is an aqueous solution comprising an alkaline earth metal source.
  • none of the separate carbonaceous feedstocks is treated with more than one type of loading solution.
  • the same feedstock of carbonaceous particulate is not contacted with the loading solution comprising a transitional metal gasification catalyst and then also contacted with the loading solution comprising an alkali metal gasification catalyst.
  • the gasification catalyst or alkaline earth metal source will associate with the carbonaceous particulate. Therefore, when each slurry is dewatered, the recovered aqueous medium will contain gasification catalyst or alkaline earth metal source that did not associate with the carbonaceous particulate.
  • the aqueous medium recovered from the dewatering contains no (or substantially no) contamination from the loading solutions used to treat the other feedstocks. Therefore, the aqueous media recovered from dewatering each sample can be reused as at least part of a loading solution without cross-contaminating the loading solutions.
  • any methods known to those skilled in the art can be used to associate the gasification catalysts or alkaline earth metal source with the carbonaceous particulate (i.e., loading).
  • Several impregnation methods known to those skilled in the art can be employed to incorporate the gasification catalysts. These methods include but are not limited to, incipient wetness impregnation, evaporative impregnation, vacuum impregnation, dip impregnation, ion exchanging, and combinations of these methods.
  • Gasification catalysts can be impregnated into the coal particulate by slurrying with a solution (e.g., aqueous) of the catalyst.
  • the solutions for slurrying the coal particulate can be prepared from fresh transition metal gasification catalyst, alkali metal gasification catalyst, and/or alkaline earth metal source, or may include amounts of transition metal gasification catalyst, alkali metal gasification catalyst, and/or alkaline earth metal source that is recycled from a previous slurrying process or from the gasification of a carbonaceous composition into a plurality of gases.
  • the contacting of the wet cake and the aqueous catalyst solution can occur at temperatures ranging from about 25 0 C to about 100 0 C, or from about 25 0 C to about 75 0 C, or from about 5O 0 C to about 75 0 C for a predetermined residence time.
  • the total amount of catalyst loaded is controlled by controlling the concentration of catalyst components in the solution, as well as the contact time, temperature and method, as can be readily determined by those of ordinary skill in the relevant art based on the characteristics of the starting coal.
  • the resulting slurries are dewatered to provide separate particulate compositions as wet cakes.
  • Methods for dewatering the slurry to provide a wet cake of the catalyzed coal particulate include filtration (gravity or vacuum), centrifugation, vibratory screening, and/or a fluid press.
  • the coal particulate is treated, via slurrying with an aqueous solution, in separate steps to provide one or more of the transition metal gasification catalyst, alkali metal catalyst, and alkaline earth source, the slurry is dewatered between each treatment step.
  • At least three separate feedstocks of carbonaceous particulate are each contacted with a loading solution. At least one carbonaceous feedstock is contacted with an aqueous solution comprising a transition metal gasification catalyst; at least one carbonaceous feedstock is contacted with an aqueous solution comprising an alkali metal gasification catalyst; and at least one carbonaceous feedstock is contacted with an aqueous solution comprising an alkaline earth metal source. In some embodiments, only feedstocks comprising (or substantially comprising) coal particulate are each contacted with a loading solution.
  • feedstocks comprising (or substantially comprising) coal particulate and at least one feedstock comprising (or substantially comprising) petroleum coke particulate are each contacted with a loading solution.
  • these feedstocks of coal particulate need not have substantially the same composition (e.g., in terms of ash content, moisture content, etc.).
  • different feedstocks of coal particulate may comprise samples of coal particulate that are compositionally different.
  • compositions of coal particulate may select various compositions of coal particulate and adjust their relative proportions to achieve a final composition that, for example, is particularly suitable for gasification of a carbonaceous particulate composition into a plurality of gaseous products in the presence of steam and under suitable temperature and pressure (e.g., in terms of ash content, moisture content, or other properties).
  • each coal feedstock is contacted with a loading solution and a petroleum coke feedstock may or may not be contacted with a loading solution.
  • the invention nevertheless encompasses embodiments where one or more additional loaded or non-loaded carbonaceous feedstocks are included in the final particulate composition.
  • additional carbonaceous feedstocks include, but are not limited to, loaded or non-loaded coal particulate, loaded or non-loaded petroleum coke particulate, loaded or non-loaded biomass, and the like, as would be apparent to one of ordinary skill in the art.
  • the invention may also encompass embodiments where additional non-carbonaceous species are included in the final composition, provided that such non-carbonaceous species would not substantially diminish the efficiency or feasibility of the gasification of the resulting carbonaceous composition, as would be apparent to one of ordinary skill in the art.
  • additional non-carbonaceous species are included in the final composition, provided that such non-carbonaceous species would not substantially diminish the efficiency or feasibility of the gasification of the resulting carbonaceous composition, as would be apparent to one of ordinary skill in the art.
  • separate feedstocks of carbonaceous particulate may be compositionally different, separate feedstocks of carbonaceous particulate may exhibit different affinities toward different loading species (e.g., transition metal gasification catalyst, alkali metal gasification catalyst, and alkaline earth metal source).
  • the preparation of the particulate composition comprises providing three separate feedstocks of coal particulate and contacting each of the three feedstocks with a different loading solution, where one loading solution comprises a transition metal gasification catalyst, another comprises an alkali metal gasification catalyst, and another comprises an alkaline earth metal source.
  • the preparation of the particulate comprises providing a petroleum coke particulate, which may or may not be contacted with a loading solution.
  • the preparation of the particulate composition comprises providing two separate feedstocks of coal particulate and one feedstock of petroleum coke particulate, and contacting each of the three feedstocks with a different loading solution, where one loading solution comprises a transition metal gasification catalyst, another comprises an alkali metal gasification catalyst, and another comprises an alkaline earth metal source.
  • one loading solution comprises a transition metal gasification catalyst
  • another comprises an alkali metal gasification catalyst
  • another comprises an alkaline earth metal source.
  • any of the three feedstocks may be contacted with any one of the three loading solutions.
  • the petroleum coke particulate can be contacted with the solution comprising the transition metal gasification catalyst, while each of the two feedstocks of coal particulate (which need not be compositionally the same) are contacted with the solution comprising the alkali metal gasification catalyst or the solution comprising the alkaline earth metal source (i.e., one coal feedstock treated with one solution and the other coal feedstock treated with the other solution).
  • the petroleum coke particulate feedstock can be contacted either the solution comprising the alkali metal gasification catalyst or the solution comprising the alkaline earth metal source, while the two coal particulate feedstocks are treated with the two loading solutions not used to treat the petroleum coke particulate feedstock (i.e., one coal feedstock treated with one solution and the other coal feedstock treated with the other solution).
  • the combining of the separate feedstocks of carbonaceous particulate may or may not be preceded by a thermal treatment step.
  • the thermally treated compositions are blended according to any methods suitable for the blending of particulate having low moisture content, including, but not limited to, kneading, and using vertical or horizontal mixers, for example, single or twin screw, ribbon, or drum mixers.
  • each dewatered slurry is blended to form a final wet cake according to any methods suitable for the blending of wet cake particulate compositions, including, but not limited to, kneading, and using vertical or horizontal mixers, for example, single or twin screw, ribbon, or drum mixers.
  • vertical or horizontal mixers for example, single or twin screw, ribbon, or drum mixers.
  • two separate loaded particulate compositions are combined together (or blended), and then the combined compositions are further combined with (or blended) with a third loaded particulate composition.
  • a coal particulate loaded with a transitional metal gasification catalyst and coal composition loaded with an alkali metal gasification catalyst are combined, and then the combined coal particulate composition is combined with a coal composition loaded with an alkaline earth metal source.
  • a coal particulate loaded with a transitional metal gasification catalyst and coal composition loaded with an alkaline earth metal source are combined, and then the combined coal particulate composition is combined with a coal composition loaded with an alkali metal gasification catalyst.
  • a coal particulate loaded with an alkaline earth metal source and coal composition loaded with an alkali metal gasification catalyst are combined, and then the combined coal particulate composition is combined with a coal composition loaded with a transition metal gasification catalyst.
  • the particulate composition typically comprises greater than about 50%, or greater than about 70%, or greater than about 85%, or greater than about 90%, of the total amount of catalyst loaded onto the coal matrix, for example, as ion-exchanged catalyst on the acidic functional groups of the coal.
  • the amount of each component associated with the coal particulate can be determined according to methods known to those skilled in the art.
  • the wet cake(s) of loaded or non- loaded carbonaceous particulate is thermally treated to achieve a suitable moisture level.
  • the residual moisture content is less than about 6 wt%, or less than about 4 wt%, or less than about 3 wt%, or less than about 2 wt%, based on the total weight of the thermally treated composition.
  • the thermal treatment may, for example, be carried out in a fluid bed slurry drier, or in any comparable apparatus known to those of skill in the art. As discussed above, the thermal treatment may be performed on each separate feedstock prior to combining the feedstocks, or may be performed after the separate feedstocks have been combined.
  • the particulate composition can be stored for future use or transferred to a feed operation for introduction into a gasification reactor.
  • the particulate composition can be conveyed to storage or feed operations according to any methods known to those skilled in the art, for example, a screw conveyer or pneumatic transport.
  • petroleum coke is dry ground, as described above, and is blended with the loaded coal particulate feedstocks while the loaded coal particulate feedstocks are in wet cake form (e.g., having not been subjected to thermal treatment).
  • the dry-ground non-loaded petroleum coke particulate may simply be blended with the wet cakes of loaded coal particulate.
  • the four feedstocks can also be blended in multiple steps.
  • two of the loaded coal compositions in wet cake form may be blended together with part of the dry-ground unloaded petcoke particulate in a first step, and then the third loaded coal composition in wet cake form and the remainder of the dry-ground unloaded petcoke particulate can be added to the mixture in a second step.
  • the number of suitable permutations for blending the multiple feedstocks in multiple steps is nearly unlimited.
  • the dry-ground unloaded petcoke particulate is blended with the loaded coal particulates in wet cake form
  • the resulting blend may or may not be thermally treated. Because the dry-ground petcoke may absorb moisture from the wet cake, the composition may not always require thermal treatment to dry the composition. Once dried by thermal treatment, the particulate composition can be stored for future use or transferred to a feed operation for introduction into a gasification reactor.
  • a petcoke particulate is wet ground and dewatered, as described above, and is then blended with the loaded coal particulate feedstocks while the loaded coal particulate is in wet cake form.
  • both the unloaded petcoke particulate and the loaded coal particulate will exist in wet cake form.
  • the various wet cakes can be blended in a single step or in multiple steps. As mentioned above, the number of suitable permutations for blending the multiple feedstocks in multiple steps is nearly unlimited.
  • dry petroleum coke particulate is mixed with at least a portion of each of the loaded coal particulate feedstocks (wet cakes) to yield three loaded wet cakes comprising loaded coal particulate and petroleum coke particulate.
  • the three wet cakes are then combined (in a single step or in multiple steps) using any suitable means known to those of skill in the art, including, but not limited to, kneading, and using vertical or horizontal mixers, for example, single or twin screw, ribbon, or drum mixers.
  • the final wet cake may or may not be thermally treated.
  • the particulate composition can be stored for future use or transferred to a feed operation for introduction into a gasification reactor.
  • the three loaded coal particulates are blended and optionally dried in any suitable order or permutation using means known to those of skill in the art (described above). Thereafter, the loaded coal particulate is combined with a dry petcoke particulate to form a particulate composition that can be stored for future use or transferred to a feed operation for introduction into a gasification reactor.
  • the particulate compositions of the present invention are particularly useful in integrated gasification processes for converting coal to combustible gases, such as methane.
  • the gasification reactors for such processes are typically operated at moderately high pressures and temperature, requiring introduction of the particulate composition to the reaction zone of the gasification reactor while maintaining the required temperature, pressure, and flow rate of the feedstock.
  • feed systems for providing feedstocks to high pressure and/or temperature environments, including, star feeders, screw feeders, rotary pistons, and lock-hoppers. It should be understood that the feed system can include two or more pressure-balanced elements, such as lock hoppers, which would be used alternately.
  • the particulate composition can be prepared at pressures conditions above the operating pressure of gasification reactor. Hence, the particulate composition can be directly passed into the gasification reactor without further pressurization.
  • Any of several catalytic gasifiers can be utilized. Suitable gasification reactors include counter-current fixed bed, co-current fixed bed, fluidized bed, entrained flow, and moving bed reactors. In one embodiment, a fluidized bed gasifier is used.
  • the particulate compositions are particularly useful for gasification at moderate temperatures of at least about 450 0 C, or of at least about 600 0 C or above, to about 900 0 C, or to about 75O 0 C, or to about 700 0 C; and at pressures of at least about 50 psig, or at least about 200 psig, or at least about 400 psig, to about 1000 psig, or to about 700 psig, or to about 600 psig.
  • the gas utilized in the gasification reactor for pressurization and reactions of the particulate composition typically comprises steam, and optionally, oxygen or air, and is supplied to the reactor according to methods known to those skilled in the art.
  • any of the steam boilers known to those skilled in the art can supply steam to the reactor.
  • Such boilers can be powered, for example, through the use of any carbonaceous material such as powdered coal, biomass etc., and including but not limited to rejected carbonaceous materials from the particulate composition preparation operation ⁇ e.g., fines, supra).
  • Steam can also be supplied from a second gasification reactor coupled to a combustion turbine where the exhaust from the reactor is thermally exchanged to a water source and produce steam.
  • the steam may be provided to the gasification reactor as described in previously incorporated US Patent Applications Serial No. , entitled "STEAM
  • Recycled steam from other process operations can also be used for supplying steam to the reactor.
  • the slurried particulate composition is dried with a fluid bed slurry drier, as discussed previously, the steam generated through vaporization can be fed to the gasification reactor.
  • the small amount of required heat input for the catalytic coal gasification reaction can be provided by superheating a gas mixture of steam and recycle gas feeding the gasification reactor by any method known to one skilled in the art.
  • compressed recycle gas of CO and H 2 can be mixed with steam and the resulting steam/recycle gas mixture can be further superheated by heat exchange with the gasification reactor effluent followed by superheating in a recycle gas furnace.
  • a methane reformer can be included in the process to supplement the recycle CO and H 2 fed to the reactor to ensure that enough recycle gas is supplied to the reactor so that the net heat of reaction is as close to neutral as possible (only slightly exothermic or endothermic), in other words, that the reaction is run under thermally neutral conditions.
  • methane can be supplied for the reformer from the methane product, as described below.
  • Reaction of the particulate composition under the described conditions typically provides a crude product gas and a char.
  • the char produced in the gasification reactor during the present processes typically is removed from the gasification reactor for sampling, purging, and/or catalyst recovery. Methods for removing char are well known to those skilled in the art. One such method taught by EP-A-0102828, for example, can be employed.
  • the char can be periodically withdrawn from the gasification reactor through a lock hopper system, although other methods are known to those skilled in the art. Processes have been developed to recover alkali metal from the solid purge in order to reduce raw material costs and to minimize environmental impact of a CCG process.
  • the char can be quenched with recycle gas and water and directed to a catalyst recycling operation for extraction and reuse of the alkali metal catalyst.
  • Particularly useful recovery and recycling processes are described in US4459138, as well as previously incorporated US4057512 and US2007/0277437A1, and previously incorporated U.S. Patent Application Serial Nos. 12/342,554, 12/342,715, 12/342,736 and 12/343,143. Reference can be had to those documents for further process details.
  • Crude product gas effluent leaving the gasification reactor can pass through a portion of the gasification reactor which serves as a disengagement zone where particles too heavy to be entrained by the gas leaving the gasification reactor (i.e., fines) are returned to the fluidized bed.
  • the disengagement zone can include one or more internal cyclone separators or similar devices for removing fines and particulates from the gas.
  • the gas effluent passing through the disengagement zone and leaving the gasification reactor generally contains CH 4 , CO 2 , H 2 and CO, H 2 S, NH3, unreacted steam, entrained fines, and other contaminants such as COS.
  • the gas stream from which the fines have been removed can then be passed through a heat exchanger to cool the gas and the recovered heat can be used to preheat recycle gas and generate high pressure steam. Residual entrained fines can also be removed by any suitable means such as external cyclone separators, optionally followed by Venturi scrubbers.
  • the recovered fines can be processed to recover alkali metal catalyst, or directly recycled back to feedstock preparation as described in previously U.S. Patent Application
  • the gas stream from which the fines have been removed can be fed to COS hydrolysis reactors for COS removal (sour process) and further cooled in a heat exchanger to recover residual heat prior to entering water scrubbers for ammonia recovery, yielding a scrubbed gas comprising at least H 2 S, CO 2 , CO, H 2 , and CH 4 .
  • Methods for COS hydrolysis are known to those skilled in the art, for example, see US4100256.
  • the residual heat from the scrubbed gas can be used to generate low pressure steam.
  • Scrubber water and sour process condensate can be processed to strip and recover H 2 S, CO 2 and NH 3 ; such processes are well known to those skilled in the art.
  • NH 3 can typically be recovered as an aqueous solution (e.g., 20 wt%).
  • a subsequent acid gas removal process can be used to remove H 2 S and CO 2 from the scrubbed gas stream by a physical absorption method involving solvent treatment of the gas to give a cleaned gas stream.
  • Such processes involve contacting the scrubbed gas with a solvent such as monoethanolamine, diethanolamine, methyldiethanolamine, diisopropylamine, diglycolamine, a solution of sodium salts of amino acids, methanol, hot potassium carbonate or the like.
  • a solvent such as monoethanolamine, diethanolamine, methyldiethanolamine, diisopropylamine, diglycolamine, a solution of sodium salts of amino acids, methanol, hot potassium carbonate or the like.
  • One method can involve the use of SELEXOL ® (UOP LLC, Des Plaines, IL USA) or RECTISOL ® (Lurgi AG, Frankfurt am Main, Germany) solvent having two trains; each train consisting of an H 2 S absorber and a CO 2 absorber.
  • the spent solvent containing H 2 S, CO 2 and other contaminants can be regenerated by any method known to those skilled in the art, including contacting the spent solvent with steam or other stripping gas to remove the contaminants or by passing the spent solvent through stripper columns.
  • Recovered acid gases can be sent for sulfur recovery processing.
  • the resulting cleaned gas stream contains mostly CH 4 , H 2 , and CO and, typically, small amounts of CO 2 and H 2 O.
  • Any recovered H 2 S from the acid gas removal and sour water stripping can be converted to elemental sulfur by any method known to those skilled in the art, including the Claus process.
  • Sulfur can be recovered as a molten liquid. Stripped water can be directed for recycled use in preparation of the catalyzed feedstock.
  • One method for removing acid gases from the scrubbed gas stream is described in previously incorporated U.S. Patent Application Serial No. , entitled "SELECTIVE REMOVAL AND RECOVERY OF ACID
  • the cleaned gas stream can be further processed to separate and recover CH 4 by any suitable gas separation method known to those skilled in the art including, but not limited to, cryogenic distillation and the use of molecular sieves or ceramic membranes, or via the generation of methane hydrate is described in previously incorporated U.S. Patent
  • a methane product stream can be produced by the gas separation process, a methane product stream and a syngas stream (H 2 and CO).
  • the syngas stream can be compressed and recycled to the gasification reactor. If necessary, a portion of the methane product can be directed to a reformer, as discussed previously and/or a portion of the methane product can be used as plant fuel.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Industrial Gases (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention porte sur des compositions particulaires comprenant un mélange intime d'un charbon et d'un catalyseur de gazéification. Les compositions particulaires sont gazéifiées en présence de vapeur d'eau pour fournir une pluralité de gaz comprenant le méthane et au moins un ou plusieurs parmi l'hydrogène, le monoxyde de carbone, le dioxyde de carbone, le sulfure d'hydrogène, l'ammoniac et autres hydrocarbures supérieurs. L'invention porte également sur des procédés pour la préparation des compositions particulaires et la conversion de la composition particulaire en une pluralité de produits gazeux.
PCT/US2009/035557 2008-02-29 2009-02-27 Compositions de charbon pour gazéification catalytique WO2009111335A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US3268808P 2008-02-29 2008-02-29
US61/032,688 2008-02-29

Publications (2)

Publication Number Publication Date
WO2009111335A2 true WO2009111335A2 (fr) 2009-09-11
WO2009111335A3 WO2009111335A3 (fr) 2010-02-25

Family

ID=40933504

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2009/035557 WO2009111335A2 (fr) 2008-02-29 2009-02-27 Compositions de charbon pour gazéification catalytique

Country Status (1)

Country Link
WO (1) WO2009111335A2 (fr)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103881755A (zh) * 2014-03-31 2014-06-25 新奥科技发展有限公司 一种原料制备装置及方法
US8999020B2 (en) 2008-04-01 2015-04-07 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US9012524B2 (en) 2011-10-06 2015-04-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9034061B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9127221B2 (en) 2011-06-03 2015-09-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9234149B2 (en) 2007-12-28 2016-01-12 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US9273260B2 (en) 2012-10-01 2016-03-01 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9328920B2 (en) 2012-10-01 2016-05-03 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
US9353322B2 (en) 2010-11-01 2016-05-31 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
CN106622394A (zh) * 2016-09-27 2017-05-10 新奥科技发展有限公司 一种复合催化剂的负载方法
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10618818B1 (en) 2019-03-22 2020-04-14 Sure Champion Investment Limited Catalytic gasification to produce ammonia and urea
CN113061476A (zh) * 2021-03-20 2021-07-02 河北烈焰机械工程有限公司 一种新型pmc固体燃料

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4094650A (en) * 1972-09-08 1978-06-13 Exxon Research & Engineering Co. Integrated catalytic gasification process
US20070000177A1 (en) * 2005-07-01 2007-01-04 Hippo Edwin J Mild catalytic steam gasification process
US20070277437A1 (en) * 2006-06-01 2007-12-06 Sheth Atul C Catalytic steam gasification process with recovery and recycle of alkali metal compounds

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4094650A (en) * 1972-09-08 1978-06-13 Exxon Research & Engineering Co. Integrated catalytic gasification process
US20070000177A1 (en) * 2005-07-01 2007-01-04 Hippo Edwin J Mild catalytic steam gasification process
US20070277437A1 (en) * 2006-06-01 2007-12-06 Sheth Atul C Catalytic steam gasification process with recovery and recycle of alkali metal compounds

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
HEINEMANN, H. ; SOMORJAI, G.A.: "Fundamental and exploratory studies of catalytic steam gasification of carbonaceous materials. Final report, fiscal years 1985--1994" 1 March 1994 (1994-03-01), XP7910414 DOI: 10.2172/10146707 Retrieved from the Internet: URL:http://www.osti.gov/energycitations/product.biblio.jsp?query_id=3&page=0&osti_id=10146707> [retrieved on 2009-11-03] *

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9234149B2 (en) 2007-12-28 2016-01-12 Greatpoint Energy, Inc. Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US8999020B2 (en) 2008-04-01 2015-04-07 Greatpoint Energy, Inc. Processes for the separation of methane from a gas stream
US9353322B2 (en) 2010-11-01 2016-05-31 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9127221B2 (en) 2011-06-03 2015-09-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9012524B2 (en) 2011-10-06 2015-04-21 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock
US9328920B2 (en) 2012-10-01 2016-05-03 Greatpoint Energy, Inc. Use of contaminated low-rank coal for combustion
US9034058B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9273260B2 (en) 2012-10-01 2016-03-01 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
US9034061B2 (en) 2012-10-01 2015-05-19 Greatpoint Energy, Inc. Agglomerated particulate low-rank coal feedstock and uses thereof
CN103881755A (zh) * 2014-03-31 2014-06-25 新奥科技发展有限公司 一种原料制备装置及方法
CN106622394A (zh) * 2016-09-27 2017-05-10 新奥科技发展有限公司 一种复合催化剂的负载方法
CN106622394B (zh) * 2016-09-27 2019-07-23 新奥科技发展有限公司 一种复合催化剂的负载方法
US10464872B1 (en) 2018-07-31 2019-11-05 Greatpoint Energy, Inc. Catalytic gasification to produce methanol
US10344231B1 (en) 2018-10-26 2019-07-09 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization
US10435637B1 (en) 2018-12-18 2019-10-08 Greatpoint Energy, Inc. Hydromethanation of a carbonaceous feedstock with improved carbon utilization and power generation
US10618818B1 (en) 2019-03-22 2020-04-14 Sure Champion Investment Limited Catalytic gasification to produce ammonia and urea
CN113061476A (zh) * 2021-03-20 2021-07-02 河北烈焰机械工程有限公司 一种新型pmc固体燃料

Also Published As

Publication number Publication date
WO2009111335A3 (fr) 2010-02-25

Similar Documents

Publication Publication Date Title
US8286901B2 (en) Coal compositions for catalytic gasification
US8297542B2 (en) Coal compositions for catalytic gasification
AU2008345189B2 (en) Petroleum coke compositions for catalytic gasification
US8114177B2 (en) Co-feed of biomass as source of makeup catalysts for catalytic coal gasification
US8652222B2 (en) Biomass compositions for catalytic gasification
US8349039B2 (en) Carbonaceous fines recycle
US9234149B2 (en) Steam generating slurry gasifier for the catalytic gasification of a carbonaceous feedstock
US8366795B2 (en) Catalytic gasification particulate compositions
AU2009262073B2 (en) Four-train catalytic gasification systems for SNG production
WO2009111335A2 (fr) Compositions de charbon pour gazéification catalytique
US20090165379A1 (en) Coal Compositions for Catalytic Gasification
US20090165384A1 (en) Continuous Process for Converting Carbonaceous Feedstock into Gaseous Products
US20090324459A1 (en) Three-Train Catalytic Gasification Systems
US20090324462A1 (en) Four-Train Catalytic Gasification Systems
WO2009158580A2 (fr) Systèmes de gazéification catalytique à quatre lignes
WO2010033846A2 (fr) Catalyseur de méthanisation de charbon de bois et son utilisation dans des procédés de gazéification
WO2009158582A2 (fr) Systèmes de gazéification catalytique à quatre lignes
WO2009111331A2 (fr) Procédé de génération de vapeur utilisant des charges de biomasse
WO2010078297A1 (fr) Procédés de préparation d'une matière particulaire carbonée catalysée

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09717715

Country of ref document: EP

Kind code of ref document: A2

NENP Non-entry into the national phase in:

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 09717715

Country of ref document: EP

Kind code of ref document: A2

点击 这是indexloc提供的php浏览器服务，不要输入任何密码和下载