WO2010117772A2 - A hot solids process having an output suitable for the input to a petrochemical process - Google Patents
A hot solids process having an output suitable for the input to a petrochemical process Download PDFInfo
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- WO2010117772A2 WO2010117772A2 PCT/US2010/029179 US2010029179W WO2010117772A2 WO 2010117772 A2 WO2010117772 A2 WO 2010117772A2 US 2010029179 W US2010029179 W US 2010029179W WO 2010117772 A2 WO2010117772 A2 WO 2010117772A2
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- reactor
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- hot solids
- petrochemical
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/02—Non-metals
-
- 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
- C10J3/02—Fixed-bed gasification of lump fuel
- C10J3/06—Continuous processes
- C10J3/12—Continuous processes using solid heat-carriers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/80—Additives
- C10G2300/805—Water
- C10G2300/807—Steam
-
- 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
- C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
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- 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
- C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
-
- 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
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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- 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
- C10J3/72—Other features
- C10J3/725—Redox processes
Definitions
- Patent Application Serial No. 61/165,042 entitled “HOT SOLIDS PROCESS SELECTIVELY OPERABLE FOR COMBUSTION PURPOSES AND GASIFICATION PURPOSES", and co-pending U.S. Provisional Patent Application 61/165,069, entitled “HOT SOLIDS PROCESS SELECTIVELY OPERABLE BASED ON THE TYPE OF APPLICATION THAT IS INVOLVED”, and co-pending U.S. Provisional Patent Application 61/165,094, entitled “HOT SOLIDS PROCESS SELECTIVELY OPERABLE BASED ON WHAT THE SPECIFIC NATURE OF THE HOT SOLIDS PROCESS' PRIMARY PURPOSE IS” all of which are incorporated herein by reference in their entirety.
- This invention relates generally to a hot solids process that is capable of generating a predetermined output that is designed to be suitable for use as an input to a petrochemical process. Moreover, the present invention relates to such a hot solids process that is designed to employ a portion of the otherwise normally unusable product output, which is produced from such a petrochemical process, for purposes of generating, in accordance with the present invention, the output from the hot solids process that is designed to be suitable for use as an input to said petrochemical process.
- the steam that is produced by steam generators, which are employed in such electrical power generation systems, from the combustion of fossil fuel therein is designed to be employed in steam turbines.
- Such steam which commonly is both at a high temperature and at a high pressure, is expanded in the aforementioned steam turbine in order to thereby effect a rotation of the steam turbine.
- Such rotation of the steam turbine in turn is operative in a known manner to cause a generator that is suitably operatively connected to the steam turbine to rotate as well. Then, when the generator undergoes such rotation, a conductor is made to move through a magnetic field thereby causing an electric current to be generated.
- the aforedescribed mode of operation is fundamentally the basis upon which electrical power generation systems continue to be predicated even to this day.
- 2,602,809 are directed to a proves, which is said to be particularly suited for the gasification of low- grade solid carbon-containing materials. More specifically, insofar as the mode of operation of the process to which the teachings of U.S. Patent No. 2,602,809 are directed is concerned, the solid carbon-containing materials are designed to be oxidized in order to convert such solid carbon-containing materials to carbon oxides by virtue of the indirect oxidation thereof with air in such a manner that the nitrogen of the air does not contaminate the product gas. Such gasification of the solid carbon-containing materials is accomplished by virtue of the alternate oxidation and reduction of a fluidized metal oxide. According to the teachings of U.S. Patent No.
- solid fuels are subjected to being converted to gases as a consequence of the contacting by a metal oxide with finely- divided solid carbon-containing materials under conditions such as to cause the metal oxide to be reduced and the carbon of the solid fuel to be oxidized to carbon oxides, with the metal oxide being the principal source of oxygen that is required for the oxidation of the carbon. Then, after the metal oxide has been reduced, the reduced metal oxide is subjected to being re-oxidized whereupon the process cycle is capable of being repeated once again.
- 4,602,573 are stated to be directed to a method of gasifying and combusting a carbonaceous fuel and, more particularly to an integrated process wherein a sulfur and nitrogen-bearing carbonaceous fuel is gasified to produce a carbon monoxide-rich low BTU fuel gas that is deigned to be subsequently combusted with additional carbonaceous fuel in a steam generator. More specifically, insofar as the mode of operation of the process to which the teachings of U. S. Patent No. 4,602,573 are directed is concerned, a first portion of sulfur and nitrogen-bearing carbonaceous fuel is gasified in a gasification reactor in a reducing atmosphere of air to produce a hot, char-containing, carbon monoxide-rich fuel gas having a low BTU content.
- a sulfur capturing material is introduced into the gasification reactor so that the gasifying of the carbonaceous fuel is carried out in the presence of the sulfur capturing material whereby a substantial portion of the sulfur in the carbonaceous fuel being gasified is captured by the sulfur capturing material.
- 4,111,158 are stated to be directed to a method of and an apparatus for carrying out an exothermic process in which a solid feed contains a combustible such as, for example, carbonaceous or sulfurous compounds.
- a combustible such as, for example, carbonaceous or sulfurous compounds.
- U.S. Patent No. 5,533,471 are considered to be representative of an exemplification of a further development in the continuing evolution of fluidized-bed combustion technologies of the type wherein hot solids processes are employed.
- teachings of U.S. Patent No. 5,533,471 are stated to be directed to a system and to a method that allow the temperature of the fluidized bed reactor to be controlled efficiently, allowing adequate heat transfer surface area for cooling of solid materials. More specifically, insofar as the mode of operation of the system and of the method to which the teachings of U.S. Patent No. 5,533,471 are directed is concerned, a circulating (fast) fluidized bed and a bubbling (slow) fluidized bed are utilized.
- these two (2) fluidized beds are mounted adjacent each other with first and second interconnections between them, typically with the fluidizing gas introducing grid of the bubbling fluidized bed being below that of the circulating fluidized bed. Because the bubbling fluidized bed has a substantially constant density throughout, with a clear demarcation line at the top thereof, the first interconnection is provided above the top of the bubbling fluidized bed so that the pressure and density conditions between the two (2) fluidized beds result in a flow of particles from the circulating fluidized bed to the bubbling fluidized bed through the first interconnection.
- the pressure and density conditions cause the particles after treatment in the bubbling fluidized bed (e.g., after the cooling of the particles therein) to return to the circulating fluidized bed through the second interconnection.
- 4,272,399 are stated to be directed to a unified process for producing high purity synthesis gas from carbon-containing materials. More specifically, insofar as the mode of operation of the unified process to which the teachings of U.S. Patent No. 4,272,399 are directed is concerned, a metal-oxygen containing material, which can be characterized as a heat and oxygen carrier and which can be referred to generally as an oxidant, is used as the transfer agent of oxygen and heat for oxidatively gasifying carbon- containing material. Continuing, steam, carbon dioxide, synthesis gas or mixtures thereof are employed to fluidize and transport the oxidant through an up-flow, co-current system.
- a metal-oxygen containing material which can be characterized as a heat and oxygen carrier and which can be referred to generally as an oxidant
- steam, carbon dioxide, synthesis gas or mixtures thereof are employed to fluidize and transport the oxidant through an up-flow, co-current system.
- synthesis gas is first oxidized and heated by the oxidant to form water and carbon dioxide in an oxidant reducing zone prior to contact of the oxidant and gases with the carbon- containing material in a gasifying zone.
- the carbon-containing materials are oxidized to predominately carbon monoxide and hydrogen in a manner such that the nitrogen contained in the air does not contaminate the product synthesis gas.
- the gasification of the carbon-containing material is accomplished by the alternate oxidation and reduction of a fluidized oxidant. Then, after such gasification, the reduced oxidant, which may be in the form of the elemental metal or lower oxidized state is re-oxidized in an oxidizing zone and the cycle is then repeated.
- a gasifier for producing a gas product from a carbonaceous fuel, which comprises a first chemical process loop including an exothermic oxidizer reactor and an endothermic reducer reactor.
- the exothermic oxidizer reactor has a CaS inlet, a hot air inlet and a CaSO4/waste gas outlet.
- the endothermic reducer reactor has a CaSO4 inlet in fluid communication with the exothermic oxidizer reactor CaSO4/waste gas outlet, a CaS/gas product outlet in fluid communication with the exothermic oxidizer reactor CaS inlet, and a materials inlet for receiving the carbonaceous fuel.
- CaS is oxidized in air in the exothermic oxidizer reactor to form hot CaSO4, which is discharged to the endothermic reducer reactor.
- hot CaSO4 and carbonaceous fuel that is received in the endothermic reducer reactor undergo an endothermic reaction utilizing the heat content of the CaSO4 with the carbonaceous fuel stripping the oxygen from the CaSO4 to form CaS and the gas product. Thereafter, the CaS is discharged to the exothermic oxidizer reactor, and with the gas product being discharged from the first chemical process loop.
- Yet another object of the present invention is to provide such a hot solids process that is relatively inexpensive to provide, is relatively uncomplicated to employ, and is characterized by its great versatility insofar as the applicability thereof to petrochemical processes is concerned.
- a hot solids process which is capable of generating a predetermined output that is designed to be suitable for use as an input to a petrochemical process.
- the mode of operation, in accordance with the present invention of such a hot solids process is such that preferably a portion of the otherwise normally unusable product output, which is produced from such a petrochemical process, is designed to be employed as an input to the hot solids process of the present invention for purposes of generating in accordance with the present invention the predetermined output from the hot solids process of the present invention, which is designed to be suitable for use as an input to said petrochemical process.
- the mode of operation of the hot solids process of the present invention is such that preferably a limestone based sorbent, such as, by way of exemplification and not limitation, CaS, is designed to be combusted in an oxidizing reactor, such oxidizing reactor preferably, by way of exemplification and not limitation, being a circulating bed reactor, which is designed to be selected from a group of reactors that includes a fixed bed reactor, a bubbling bed reactor, a circulating bed reactor, a transport reactor, and an entrained bed reactor, in order to thereby produce hot CaS 04 from the combustion of such limestone based sorbent.
- a limestone based sorbent such as, by way of exemplification and not limitation, CaS
- This hot CaSO4 is then in turn designed to be employed in a reducing reactor, such reducing reactor preferably, by way of exemplification and not limitation, being a circulating bed reactor, which is designed to be selected from a group of reactors that includes a fixed bed reactor, a bubbling bed reactor, a circulating bed reactor, a transport reactor, and an entrained bed reactor, for purposes of generating the predetermined output, which is designed to be suitable for use as an input to a petrochemical process.
- a reducing reactor such preferably, by way of exemplification and not limitation, being a circulating bed reactor, which is designed to be selected from a group of reactors that includes a fixed bed reactor, a bubbling bed reactor, a circulating bed reactor, a transport reactor, and an entrained bed reactor, for purposes of generating the predetermined output, which is designed to be suitable for use as an input to a petrochemical process.
- the inputs to the oxidizing reactor which is employed in accordance with the mode of operation of the hot solids process of the present invention, when the fuel that is designed to be combusted in accordance therewith comprises a carbonaceous fuel, such as, preferably a portion of the otherwise normally unusable product output, which is produced from a petrochemical process, and wherein a portion of such otherwise normally unusable product output, which is produced from a petrochemical process, and which more particularly comprises petcoke and/or oil residuals that are known to be otherwise produced as normally unusable product outputs from a petrochemical process, and when the predetermined output that is being generated in accordance with the preferred mode of operation of the hot solids process of the present invention is designed to be suitable for use as an input to a petrochemical process, include CaS and air, and the outputs from such an oxidizing reactor in such a case include ash, CaSO4, and N
- the inputs to the reducing reactor which is employed in accordance with the mode of operation of the hot solids process of the present invention, when the fuel that is designed to be combusted in accordance therewith comprises a carbonaceous fuel, such as, preferably a portion of the otherwise normally unusable product output, which is produced from a petrochemical process, and wherein a portion of such otherwise normally unusable product output, which is produced from a petrochemical process, and which more particularly comprises petcoke and/or oil residuals that are known to be otherwise produced as normally unusable product outputs from a petrochemical process, and when the predetermined output that is being generated in accordance with the preferred mode of operation of the hot solids process of the present invention is designed to be suitable for use as an input to a petrochemical process, include the carbonaceous fuel, CaCC ⁇ , steam, and CaSO4, and the output from such a reducing reactor in such a case is designed to be the predetermined output, which is being generated in accordance with the preferred
- Figure 1 of the drawing is a schematic diagram of a preferred embodiment of the mode of operation of a hot solids process that functions in accordance with the present invention to generate a predetermined output, which is suitable for use as an input to a petrochemical process, the latter petrochemical process also being schematically depicted as well in Figure 1.
- FIG. 1 of the drawing there is depicted therein a schematic diagram of a hot solids process, generally denoted by the reference numeral 10 in Figure 1 of the drawing, that is designed to be operable in accordance with the present invention for purposes of generating a predetermined output, such as, by way of exemplification and not limitation, H2 or syngas and steam, and with the latter predetermined output being denoted by the arrow 12 in Figure 1 of the drawing.
- the predetermined output 12 from the hot solids process 10 is designed in accordance with the present invention to be suitable for use as an input to a petrochemical process, the latter petrochemical process being denoted generally by the reference numeral 14 in Figure 1 of the drawing.
- the mode of operation, in accordance with the present invention of the hot solids process 10 is such that preferably a portion of the otherwise normally unusable product output, denoted by the reference numeral 16 in Figure 1 of the drawing, which is produced from the petrochemical process 14, is designed to be utilized as an input to the hot solids process 10 of the present invention for purposes of generating in accordance with the present invention the predetermined output 12 from the hot solids process 10 of the present invention that is designed to be suitable for use as an input to the petrochemical process, which is schematically depicted at 14 in Figure 1 of the drawing.
- the hot solids process of the present invention in accordance with the preferred mode of operation thereof is designed to utilize air; a carbonaceous fuel, such as, by way of exemplification and not limitation, the portion of the otherwise normally unusable product output, which is 16 from a petrochemical process, such as, the petrochemical process that is schematically depicted at 14 in Figure 1 of the drawing, and wherein such a portion of the otherwise normally unusable product output 16, which is produced from the petrochemical process 14, and which preferably comprises petcoke and/or oil residuals that are known to be producible as an otherwise normally unusable product output from a petrochemical process, such as, the petrochemical process 14 that is schematically depicted in Figure 1 of the drawing; a source of calcium (e.g., calcium oxide); and steam to effect therewith the generation of the predetermined output 12, which is designed to be suitable for use as an input to a petrochemical process, such as, the petrochemical process that is schematically depicte
- a reducing reactor denoted generally by the reference numeral 18 in Figure 1 of the drawing, selected from a group of reactors that includes a fixed bed reactor, a bubbling bed reactor, a circulating bed reactor, a transport reactor and an entrained bed reactor and preferably comprising a circulating bed reactor
- an oxidizing reactor denoted generally by the reference numeral 20 in Figure 1 of the drawing, selected from a group of reactors that includes a fixed bed reactor, a bubbling bed reactor, a circulating bed reactor, a transport reactor and an entrained bed reactor and preferably comprising a circulating bed reactor, are each designed to be employed in the hot solids process 10 of the present invention, in accordance with the preferred mode of operation thereof.
- the carbonaceous fuel such as, by way of exemplification and not limitation, the portion of the otherwise normally unusable product output 16 that is produced from the petrochemical process, which is schematically depicted at 14 in Figure 1 of the drawing, that is designed to be supplied from the petrochemical process 14 as an input to the reducing reactor 18, is designed to be burned in the reducing reactor 18 preferably using air indirectly.
- a source of calcium i.e., calcium oxide
- the latter source of calcium is also supplied, by way of exemplification and not limitation, as an input to the reducing reactor 18.
- source of calcium 22 could equally well be supplied elsewhere in the hot solids process 10 of the present invention other than as an input to the reducing reactor 18, without departing from the essence of the present invention.
- Such source of calcium 22 which may be selected from the group including of limestone (CaCC ⁇ ) or lime (CaO) or gypsum or the spent bed material from a circulating bed boiler, by way of exemplification and not limitation, preferably comprises limestone (CaCC ⁇ ).
- limestone (CaCO3) 22 which is added in accordance with the preferred mode of operation of the hot solids process 10 of the present invention, is designed to be operative to capture in the reducing reactor 18 the sulfur (S), which is contained in the carbonaceous fuel 16, such as to thereby produce calcium sulfide (CaS) therefrom in the reducing reactor 18.
- S sulfur
- CaS calcium sulfide
- Such calcium sulfide (CaS) as denoted by the arrow 24 in
- FIG. 1 of the drawing is then made to exit from the reducing reactor 18 as an output therefrom, whereupon such calcium sulfide (CaS) 24 is designed to be supplied as an input to the oxidizing reactor 20.
- this calcium sulfide (CaS) 24 is designed to be burned in a heat liberation reaction with air, and with the latter air being denoted by the arrow 26 in Figure 1 of the drawing, which is designed to be supplied as an input to the oxidizing reactor 20, such as to thereby effect the production therefrom of calcium sulfate (CaSO4) in the oxidizing reactor 20.
- This calcium sulfate (CaSO4) is then designed to be made to exit as an output from the oxidizing reactor 20, whereupon this calcium sulfate (CaSO4) 28 is designed to be cycled to the reducing reactor 18 as an input thereto for purposes of thereby producing therefrom the supply of oxygen and of heat that is required both in order to burn the carbonaceous fuel 16 and in order to reduce the calcium sulfate (CaSO4) 28 to calcium sulfide (CaS) 24 in the reducing reactor 18, such as to thereby permit a continuous recycling thereof to be had.
- CaSO4 calcium sulfate
- steam is preferably also supplied as an input to the reducing reactor 18.
- the burning of the carbonaceous fuel 16 in the reducing reactor 18 is designed to be such that the predetermined output 12 is thus capable of being generated in the reducing reactor 18, and with the carbon and the hydrogen contained in the carbonaceous fuel 16 being converted, in the course of such burning of the carbonaceous fuel 16 to a product gas, such as, H2 or syngas, in a suitable form such that such product gas, with the possible addition thereto of steam is capable of being made to function as the predetermined output 12 from the hot solids process 10 of the present invention, in accordance with the preferred mode of operation thereof, which is designed to be suitable for use as an input to a petrochemical process, such as, by way of exemplification and not limitation, the predetermined process, which is schematically depicted at 14 in Figure 1 of the drawing.
- a product gas such as, H2 or syngas
- the nitrogen (N2) which remains from the oxidation of the calcium sulfide (CaS) 24 that takes place in the oxidizing reactor 20, is designed to be made to exit through an outlet (not shown in the interest of maintaining clarity of illustration in the drawing) with which the oxidizing reactor 20 is designed to be suitably provided for this purpose.
- the hot solids process 10 is suitably constructed so as to be capable of generating a predetermined output 12, such as, by way of exemplification and not limitation, steam and H2 or syngas, that is designed to be suitable for use as an input to a petrochemical process, such as, for example, the petrochemical process, which is schematically depicted in Figure 1 of the drawing.
- a predetermined output 12 such as, by way of exemplification and not limitation, steam and H2 or syngas
- the crude 34 and the input 12, the latter being produced as an output from the hot solids process 10 of the present invention are designed to be supplied as inputs to the petrochemical process 14 such that in accordance with conventional practice the crude 34 and the input 12, which are supplied as inputs to the petrochemical process 14, are designed to be converted in known fashion through operation of the petrochemical process 14 so as to thereby produce both a usable product output, the latter usable product output being denoted by the arrow 36 in Figure 1 of the drawing,, that commonly consists of one or more of the following: diesel fuel, gasoline, etc., and an otherwise normally unusable product output 16 to which reference has been had herein previously.
- a portion of the otherwise normally unusable product output 16, which preferably comprises, by way of exemplification and not limitation, petcoke and/or oil residuals, from the petrochemical process that is depicted at 14 in Figure 1 of the drawing, is designed to be employed in accordance with the present invention as an input to the hot solids process 10 for purposes of effecting, in accordance with the present invention, the production within the hot solids process 10 of the predetermined output 12 that is designed to be suitable for purposes of being employed as the input 12 to the petrochemical process, which is schematically depicted at 14 in Figure 1 of the drawing.
- the oxide may include a metal oxide, for example, formed of iron such as FeO.
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP10723424A EP2414486A2 (en) | 2009-03-31 | 2010-03-30 | A hot solids process having an output suitable for the input to a petrochemical process |
CA2757824A CA2757824C (en) | 2009-03-31 | 2010-03-30 | A hot solids process having an output suitable for the input to a petrochemical process |
CN2010800158212A CN102459524A (en) | 2009-03-31 | 2010-03-30 | A hot solids process having an output suitable for the input to a petrochemical process |
JP2012503600A JP2012522120A (en) | 2009-03-31 | 2010-03-30 | High temperature solid process with output suitable for input to petrochemical process |
AU2010234835A AU2010234835A1 (en) | 2009-03-31 | 2010-03-30 | A hot solids process having an output suitable for the input to a petrochemical process |
Applications Claiming Priority (8)
Application Number | Priority Date | Filing Date | Title |
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US16509409P | 2009-03-31 | 2009-03-31 | |
US16504209P | 2009-03-31 | 2009-03-31 | |
US16506909P | 2009-03-31 | 2009-03-31 | |
US61/165,042 | 2009-03-31 | ||
US61/165,069 | 2009-03-31 | ||
US61/165,094 | 2009-03-31 | ||
US12/749,238 | 2010-03-29 | ||
US12/749,238 US20100288678A1 (en) | 2009-03-31 | 2010-03-29 | Hot solids process having an output suitable for the input to a petrochemical process |
Publications (2)
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WO2010117772A2 true WO2010117772A2 (en) | 2010-10-14 |
WO2010117772A3 WO2010117772A3 (en) | 2011-04-07 |
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PCT/US2010/029179 WO2010117772A2 (en) | 2009-03-31 | 2010-03-30 | A hot solids process having an output suitable for the input to a petrochemical process |
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US (1) | US20100288678A1 (en) |
EP (1) | EP2414486A2 (en) |
JP (1) | JP2012522120A (en) |
CN (1) | CN102459524A (en) |
AU (1) | AU2010234835A1 (en) |
CA (1) | CA2757824C (en) |
WO (1) | WO2010117772A2 (en) |
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US4309198A (en) | 1979-01-09 | 1982-01-05 | Exxon Research & Engineering Co. | Method of converting liquid and/or solid fuel to a substantially inerts-free gas |
US4704136A (en) | 1984-06-04 | 1987-11-03 | Freeport-Mcmoran Resource Partners, Limited Partnership | Sulfate reduction process useful in coal gasification |
US7083658B2 (en) | 2003-05-29 | 2006-08-01 | Alstom Technology Ltd | Hot solids gasifier with CO2 removal and hydrogen production |
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US2602809A (en) * | 1948-07-10 | 1952-07-08 | Kellogg M W Co | Treatment of solid carbon containing materials to produce carbon monoxide for the synthesis of organic materials |
US3969089A (en) * | 1971-11-12 | 1976-07-13 | Exxon Research And Engineering Company | Manufacture of combustible gases |
DE2624302A1 (en) * | 1976-05-31 | 1977-12-22 | Metallgesellschaft Ag | PROCEDURE FOR CARRYING OUT EXOTHERMAL PROCESSES |
US4272399A (en) * | 1979-09-21 | 1981-06-09 | Monsanto Company | Conversion of carbon-containing materials to synthesis gas |
US4602573A (en) * | 1985-02-22 | 1986-07-29 | Combustion Engineering, Inc. | Integrated process for gasifying and combusting a carbonaceous fuel |
GB8600615D0 (en) * | 1986-01-11 | 1986-02-19 | Moss G | Non-polluting method of burning fuel |
CA2127394A1 (en) * | 1993-07-12 | 1995-01-13 | William Martin Campbell | Transport gasifier |
US6083862A (en) * | 1994-03-14 | 2000-07-04 | Iowa State University Research Foundation, Inc. | Cyclic process for oxidation of calcium sulfide |
US5533471A (en) * | 1994-08-17 | 1996-07-09 | A. Ahlstrom Corporation | fluidized bed reactor and method of operation thereof |
EP1567618A2 (en) * | 2002-05-22 | 2005-08-31 | Manufacturing And Technology Conversion International, Inc. | Pulse gasification and hot gas cleanup apparatus and process |
US20070000177A1 (en) * | 2005-07-01 | 2007-01-04 | Hippo Edwin J | Mild catalytic steam gasification process |
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2010
- 2010-03-29 US US12/749,238 patent/US20100288678A1/en not_active Abandoned
- 2010-03-30 WO PCT/US2010/029179 patent/WO2010117772A2/en active Application Filing
- 2010-03-30 EP EP10723424A patent/EP2414486A2/en not_active Withdrawn
- 2010-03-30 JP JP2012503600A patent/JP2012522120A/en not_active Withdrawn
- 2010-03-30 AU AU2010234835A patent/AU2010234835A1/en not_active Abandoned
- 2010-03-30 CN CN2010800158212A patent/CN102459524A/en active Pending
- 2010-03-30 CA CA2757824A patent/CA2757824C/en not_active Expired - Fee Related
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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US4309198A (en) | 1979-01-09 | 1982-01-05 | Exxon Research & Engineering Co. | Method of converting liquid and/or solid fuel to a substantially inerts-free gas |
US4704136A (en) | 1984-06-04 | 1987-11-03 | Freeport-Mcmoran Resource Partners, Limited Partnership | Sulfate reduction process useful in coal gasification |
US7083658B2 (en) | 2003-05-29 | 2006-08-01 | Alstom Technology Ltd | Hot solids gasifier with CO2 removal and hydrogen production |
Non-Patent Citations (1)
Title |
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See also references of EP2414486A2 |
Also Published As
Publication number | Publication date |
---|---|
WO2010117772A3 (en) | 2011-04-07 |
EP2414486A2 (en) | 2012-02-08 |
CN102459524A (en) | 2012-05-16 |
US20100288678A1 (en) | 2010-11-18 |
JP2012522120A (en) | 2012-09-20 |
CA2757824A1 (en) | 2010-10-14 |
AU2010234835A1 (en) | 2011-10-27 |
CA2757824C (en) | 2013-12-03 |
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