WO2006113673A2 - Procedes et systemes de reduction d'emissions - Google Patents

Procedes et systemes de reduction d'emissions Download PDF

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Publication number
WO2006113673A2
WO2006113673A2 PCT/US2006/014495 US2006014495W WO2006113673A2 WO 2006113673 A2 WO2006113673 A2 WO 2006113673A2 US 2006014495 W US2006014495 W US 2006014495W WO 2006113673 A2 WO2006113673 A2 WO 2006113673A2
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Prior art keywords
carbon dioxide
lime
kiln
limestone
heat
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Ceased
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PCT/US2006/014495
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English (en)
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WO2006113673A3 (fr
Inventor
Klaus S. Lackner
Frank S. Zeman
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Columbia University in the City of New York
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Columbia University in the City of New York
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Application filed by Columbia University in the City of New York filed Critical Columbia University in the City of New York
Priority to EP06769839A priority Critical patent/EP1879693A4/fr
Publication of WO2006113673A2 publication Critical patent/WO2006113673A2/fr
Publication of WO2006113673A3 publication Critical patent/WO2006113673A3/fr
Priority to US11/874,743 priority patent/US20130213280A9/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • B01J20/041—Oxides or hydroxides
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B2/00—Lime, magnesia or dolomite
    • C04B2/10—Preheating, burning calcining or cooling
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • C04B7/367—Avoiding or minimising carbon dioxide emissions
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/10—Arrangements for using waste heat
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
    • F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
    • F27D17/20—Arrangements for treatment or cleaning of waste gases
    • F27D17/22—Arrangements for treatment or cleaning of waste gases for removing solid constituents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/602—Oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B7/00—Rotary-drum furnaces, i.e. horizontal or slightly inclined
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/10—Production of cement, e.g. improving or optimising the production methods; Cement grinding
    • Y02P40/18—Carbon capture and storage [CCS]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P40/00—Technologies relating to the processing of minerals
    • Y02P40/40—Production or processing of lime, e.g. limestone regeneration of lime in pulp and sugar mills

Definitions

  • the invention relates to methods and systems for reducing emissions.
  • the invention relates to kilns having reduced emissions.
  • the invention also relates to methods and systems for improving the efficiency of a combustion system.
  • the invention further relates to methods and systems for capturing carbon dioxide from a combustion system.
  • the invention relates to methods and systems for reducing carbon dioxide emission.
  • the invention relates to reduced carbon dioxide emission kilns having a calcination zone for converting limestone into lime and carbon dioxide gas; an oxygen inlet; and a fuel inlet.
  • the heat carbon dioxide can be recycled back into the kiln via and/or it can be captured to reduce the carbon dioxide emission.
  • the invention relates to heat-exchange systems having a heat-release zone for reacting lime and steam to generate slaked lime in an exothermic process; and a heat-absorption zone that is heated by a heat source to transform the slaked lime back into lime and steam.
  • the lime and steam produced in the heat-absorption zone can be recycled back into the heat release zone.
  • the heat generated in the exothermic process may be utilized to dry fuel entering a combustion system or to increase the efficiency of one or more power generating systems.
  • the power generating system can be a turbine power plant for generating electricity and the heat generated in the exothermic process can be utilized to heat feedwater for driving one or more turbines of the turbine power plant.
  • the invention relates to methods for improving the efficiency of a combustion system.
  • the methods of the invention can include (a) combining lime and steam to form slaked lime in an exothermic process; (b) utilizing heat generated by the exothermic process to increase the efficiency of the combustion system or to increase the efficiency of a different power generating system (e.g., to heat feedwater for driving one or more turbines in a turbine power plant); (c) utilizing a heated exhaust gas from the combustion system to heat the slaked lime generated in step (a), resulting in the formation of lime and steam; and (d) utilizing the lime and steam generated in step (c) to repeat the process of step (a).
  • the combustion system can be at a temperature greater than 500 0 C.
  • the heat generated by the exothermic process can be utilized to dry solids entering the combustion system.
  • the invention relates to methods for capturing carbon dioxide from a combustion system.
  • the methods of the invention can include (a) contacting carbon dioxide from an exhaust gas of the combustion system with slaked lime to form limestone; (b) heating the limestone to form lime and carbon dioxide; and (c) capturing the carbon dioxide generated in step (b).
  • FIG. 1 shows a process schematic diagram of methods and systems for combusting carbonaceous fuel with reduced emissions in accordance with certain embodiments of the invention
  • FIG. 2 shows a process schematic diagram of methods and systems for exchanging heat in accordance with certain embodiments of the invention
  • FIG. 3 shows a graph of the mass loss that occurs as slaked lime (Ca(OH) 2 ) is heated in a heat absorption zone in accordance with certain embodiments of the invention
  • FIG. 4 shows a graph of the mass increase that occurs when lime (CaO) and slaked lime (Ca(OH) 2 ) are contacted with carbon dioxide (CO 2 ) in accordance with certain embodiments of the invention;
  • FIG. 5 shows a process schematic diagram of a reduced emission kiln in accordance with certain embodiments of the invention
  • FIG. 6 shows a graph comparing the conversion of lime (CaO) and slaked lime (Ca(OH) 2 ) into limestone in accordance with certain embodiments of the invention; and [0019]
  • FIG. 7 shows another process schematic diagram of methods and systems for combusting carbonaceous fuel with reduced emissions in accordance with certain embodiments of the invention.
  • lime refers to a material predominantly composed of CaO.
  • soda lime refers to a material predominantly composed of Ca(OH) 2 .
  • limestone refers to a material predominantly composed of CaCO 3 .
  • the term “limestone” may refer to a material having CaCO 3 and MgCO 3 (dolomite).
  • the terms "reduced carbon dioxide emission kiln" and related term as used herein can include a kiln wherein the kiln's total carbon dioxide emissions into the environment outside of the kiln are less than about 1% or 10,000 ppm of the total gas in the system.
  • the kiln releases about 10,000 ppm, about 1,000 ppm, about 100 ppm, about 10 ppm, 9 ppm, about 8 ppm, about 7 ppm, about 6 ppm, about 5 ppm, about 4 ppm, about 3 ppm, about 2 ppm, about 1 ppm, or about 0 ppm of carbon dioxide into the environment outside of the kiln.
  • the kiln does not release any carbon dioxide into the environment outside of the kiln.
  • carbonaceous fuel can include, but are not limited to, coal, fuel oil, natural gas, petro-coke, waste oil, a gaseous hydrocarbon, such as methane, ethane, propane or butane, tires, or biomass.
  • a combustion system 10 such as a carbonaceous fuel combustion system, may contain a combustion zone 101 for burning carbonaceous fuel.
  • the combustion system 10 may be a boiler where the combustion zone 101 is heated to temperatures greater than about 1000 0 C.
  • solid ash may be created and removed from the bottom of the combustion zone 101.
  • Burning of the carbonaceous fuel can further generate a heated gas stream 102 that contains carbon dioxide, fly ash, and other contaminants (such as sulfur dioxide (SO 2 ) gas).
  • the heated gas stream 102 may indirectly heat pipes 103 containing, for example, steam, which can then drive one or more turbines (not shown) to generate power, such as electricity.
  • gas stream 102 From the combustion zone 101, gas stream 102 can pass through a particle separator 105, heat-exchange system 107, contaminant removal system 109, and carbon dioxide capture system 111.
  • Particle Separator 105 Particle Separator 105
  • Particle separator 105 may be any suitable particle separator capable of removing particulate matters, such as fly ash.
  • particle separator 105 maybe an electrostatic precipitator or filters.
  • the invention provides a heat-exchange system 107 useful for improving the efficiency of a combustion system.
  • heat-exchange system 107 may further extract additional heat that was not extracted through pipes 103 and used for any desired processes as described herein.
  • heat-exchange system 107 may be based on a calcium-driven heat-exchange process.
  • gas stream 102 may indirectly contact or pass over a heat absorption zone 201 (e.g., made of tubes) that contains steam and slaked lime.
  • a heat absorption zone 201 e.g., made of tubes
  • gas stream 102 can initially be at a temperature above about 500 °C, 550 °C, 600 °C, 700 °C, 800 0 C, or 900 0 C.
  • Heat from gas stream 102 may be transferred to heat absorption zone 201 and slaked lime can be converted to lime and steam as shown in Equation [3].
  • the temperature of the resulting lime and/or steam may be above about 100 °C, 200 °C, 300 0 C, 400 0 C, 500 0 C, 550 °C, 600 °C, 700 °C, 800 °C, or 900 °C.
  • heat absorption zone 201 may absorb up to about 100 % of the heat from gas stream 102.
  • Heat-exchange system 107 can further contain a heat release zone 203, wherein lime and steam obtained from reaction [3] combine to form slaked lime in an exothermic process as shown in Equation [4].
  • the heat generated by the exothermic process can be used elsewhere in the system and can be transported via one or more heat exchangers 205.
  • heat-exchange system 107 can be integrally incorporated within the combustion system 10.
  • gas stream 102 may pass over heat absorption zone 201 and the heat generated by the exothermic process of Equation [4] can be utilized to dry solids entering the combustion system 10.
  • the heat generated by the exothermic process of Equation [4] can be utilized to heat the feedwater to drive the one or more turbines for generating electricity.
  • the heat absorption zone 201, heat release zone 203, and heat exchangers 205 is not necessarily limited as a component of the combustion system 10 and may be embodied as a separate component that may be used in any suitable systems or processes.
  • any heat containing substance may be contact or pass over the heat absorption zone 201 and the heat generated by the exothermic process of Equation [4] can be utilized in any desired process, such as to heat feedwater for another process.
  • the calcium-driven heat exchanger and methods for improving the efficiency of a combustion system can be used to improve the efficiency of a Fischer-Tropsch process.
  • FIG. 3 shows an experimental graph of the mass loss that occurs as slaked lime is heated under nitrogen conditions to demonstrate the feasibility of the heat absorption zone 201.
  • a concomitant drop in mass begins about 400 0 C. This drop may correspond the onset of reaction shown in Equation [3], after which the mass stays relatively constant. It should be noted that at about 700-750 °C, a smaller, albeit noticeable, drop in mass occurs, which may correspond to a reaction that occurs on limestone that may have been present initially in the sample (FIG. 3 further shows a similar mass loss of pure limestone around 700 °C).
  • Contaminant removal system 109 may be any suitable system capable of removing or capturing contaminants, such as sulfur dioxide.
  • suitable system capable of removing or capturing contaminants, such as sulfur dioxide.
  • dry sorbent scrubbers or lime spraying can be utilized.
  • limestone pellets can be introduced to the top of a tank where the surface of the limestone pellets reacts with contaminants (e.g. sulfur dioxide) contained in gas stream 102.
  • the reacted pellets can fall down into a hopper and then fed into a device that scrapes the reacted outside layer of the limestone pellets.
  • the regenerated limestone pellet can be fed back to the top of the tank and the scrubbing may be repeated.
  • lime spraying powdered lime, either in the dry state or mixed with water to form a paste, can be used.
  • the lime can be sprayed into the gas stream 102 inside a reaction chamber where it reacts with the contaminants. For example, if sulfur dioxide is the predominant contaminant to be removed, lime may turn into gypsum, which can be captured for use in other processes.
  • the invention also provides a carbon dioxide capture system 111 useful for reducing emission of carbon dioxide from combustion systems 10.
  • carbon dioxide capture system 111 can include means for contacting carbon dioxide with lime as shown in Equation [5].
  • carbon dioxide capture system 111 may include means for contacting carbon dioxide with slaked lime as shown in Equation [6].
  • means for contacting carbon dioxide with lime or slaked lime may include a chamber, a tube, a container, or the like having holes that allow passage of carbon dioxide into and out of the chamber, tube, container, or the like.
  • Means for contacting carbon dioxide with lime or slaked lime may also include a fluidized bed or circulating fluidized bed wherein lime or slaked lime are suspended on upward blowing stream of carbon dioxide.
  • This system can also include a bubbling fluidized bed.
  • Such systems may also include cyclones that separate the solids and residual exhaust or flue gas.
  • FIG. 4 shows the amount of mass increase that occurs as a function of temperature when lime and slaked lime are contacted with carbon dioxide. As shown, a significant increase in mass occurs from about 350 0 C. FIG. 4 shows an uptake of carbon dioxide up to about 30% the initial weight of lime or slaked lime.
  • combustion system 10 can further include a sorbent regeneration system 113 for regenerating the sorbent material.
  • the limestone generated in the carbon dioxide capture system 111 may be converted back into lime, as shown in Equation [7], and recycled back to the carbon dioxide capture system 111.
  • the sorbent regeneration system 113 may be a kiln having reduced emissions.
  • the sorbent regeneration system 113 may be an oxygen-fired, reduced carbon dioxide emission kiln 50.
  • the reduced emission kiln 50 may be integrally incorporated in combustion system 10 or may function as a separate device operably connected with the combustion system 10.
  • the reduced emission kiln 50 may be operating independently as a reduced emission lime kiln.
  • reduced emission kiln 50 can be utilized to produce lime and replace traditional lime kilns having higher carbon dioxide emissions.
  • the reduced emission kiln 50 can include an inlet 501 for providing a gas containing oxygen (or pure oxygen), a fuel inlet 503 for providing a fuel source (e.g., carbonaceous fuel such as carbon), a limestone inlet 505 for receiving the limestone from the carbon dioxide capture system 111, and a calcination zone 507 for converting the limestone feedstock into lime and heated carbon dioxide gas.
  • the reduced emission kiln 50 can further contain a carbon dioxide recycle inlet 509 for recirculating the heated carbon dioxide gas produced in the calcination zone 507 back into the reduced emission kiln 50.
  • the heated carbon dioxide produced in the calcination zone 507 can be captured for subsequent sequestration.
  • the limestone may be preheated in a preheating zone 511 before entering the calcination zone 507.
  • the preheating zone 511 may be heated using the heated carbon dioxide gas produced in the calcination zone 507 or using an auxiliary heating source.
  • the limestone feedstock can be preheated in the preheating zone 511 using heated exhaust gases from a combustion process that takes place outside of the reduced emission kiln 50 (e.g., heat derived from combustion zone 101 or heat exchanger 205). Preheating the limestone feedstock may allow the reduced emission kiln to operate with higher efficiency.
  • the reduced emission kiln 50 can also include a gasification zone to convert various non-gaseous fuels to a gas prior to burning.
  • the carbon dioxide produced in the calcination zone 507 may be utilized to gasify the carbonaceous fuel in a gasification zone 513 according to the Boudouard reaction shown in Equation [8].
  • the various non-gaseous fuels can include, but are not limited to, carbonaceous fuel.
  • coal may be gasified prior to burning in the reduced emission kiln 50.
  • carbon dioxide produced in the calcination zone 507 can be recycled and used as a flood gas to temper the combustion reaction taking place in the kiln.
  • use of high purity oxygen for combustion may excessively raise the temperature of the kiln and hot carbon dioxide gas may be utilized to temper the flame temperature.
  • the calcination zone 507 may be a fluidized bed that avoids mixing air with the carbon dioxide produced in a calcination process.
  • oxygen can enter the calciner through a mixed solid oxide membrane that separates the fluidized bed from the input air.
  • the calciner can be fluidized using a stream of gases, such as methane or carbon dioxide, and the heat of combustion can be transferred to the reactive materials.
  • the fluidized bed can operate at temperatures ranging from about room temperature to about 1000 0 C.
  • the fluidized bed may produce a pure stream of carbon dioxide and the calcined product, such as lime.
  • fluidized bed includes, but is not limited to, recycling sorbent materials created in the capture of carbon dioxide.
  • the fluidized bed may also be used for recycling metal oxide sorbent materials used in industrial processes such as power plants or in any other process that uses high-temperature fluidized beds, such as the manufacture of cement.
  • an oxygen-blown reduced emission kiln of the invention include, but are not limited to, the production of lime, clinker, and cement with reduced carbon dioxide emissions; reducing the emissions from power plants which are run on coal or one or more fossil fuels; reducing the carbon dioxide emissions from iron and steel blast furnaces; in the paper industry for paper production processes with reduced emissions; for performing Fischer-Tropsch processes with reduced carbon dioxide emissions; or to reduce carbon dioxide emissions in a system used for the heat treatment of solids or the volatilization of pollutants, such as a soil remediation method in which soil is burned to oxidize pollutants.
  • the oxygen-blown reduced emission kiln of the invention may be utilized to capture the carbon dioxide gases contained in the exhaust gas of one or more of the processes described above.
  • lime may further be hydrated into slaked lime, as shown in Equation [9], before being recycled back to the carbon dioxide capture system 111.
  • FIG. 6 shows a graph comparing the conversion of lime (bottom curve labeled as CaO; reproduced from Abanade, J.C., "The maximum capture efficiency of CO 2 using a carbonation/calcination cycle of CaO/CaCO 3 ,” Chemical Engineering Journal, vol. 90, (2002), pp. 303-306) and slaked lime (top curve labeled as Ca(OH) 2 ) into limestone as a function of the number of regeneration cycle. As shown, only 40% of lime is converted to limestone after five regeneration cycles whereas >90% conversion of slaked lime into limestone is still observed after five regeneration cycles. Slaked lime appears to demonstrate superior results over lime, which is unexpected.
  • lime generated in the calcination zone 507 may be transported via outlet 515 to a reaction chamber (not shown) where a hydration reaction shown in Equation [9] can be carried out. Slaked lime can then be sent into the carbon dioxide capture system 111 to improve carbon dioxide capture and to reduce emissions.
  • combustion system 10 may be designed as shown in FIG. 7. As shown, heat generated in combustion zone 101 may be utilized to drive a multi-stage turbine system 701 via steam and generate electricity.
  • the emission gases generated from the combustion zone may be captured via a carbon dioxide capture system 111.
  • carbon dioxide capture system 111 slaked lime maybe situated in a manner to directly contact and hence capture the carbon dioxide emission before it leaves the stack (see Equations [5] or [6]).
  • the converted limestone may be transported to calcination zone 703 which is located near the combustion zone 101 to form lime and carbon dioxide according to reaction shown in Equation [7].
  • the carbon dioxide gas maybe removed or captured from the product stream by any suitable means.
  • the phase difference between the gaseous carbon dioxide and the solid lime may be utilized to separate the carbon dioxide gas and preferentially remove or capture the carbon dioxide gas.
  • the solid lime may be transported to a hydration chamber 705 to be combined with steam to form slaked lime according to reaction shown in Equation [9].
  • the generated slaked lime may then be transported to the carbon dioxide capture system 111 and continuously recycled as shown.
  • the carbon dioxide capture system 111 utilizes lime rather than slaked lime, lime may be directly recycled to the carbon dioxide capture system 111 without passing through the hydration chamber 705.
  • energy released in the exothermic reaction occurring in hydration chamber 705 may further be extracted to aid in driving the multi-stage turbine system 701.
  • heat exchangers 707 may be provided between hydration chamber 705 and the multi-stage turbine system 701 after the steam has expanded in a first turbine to allow driving a second turbine shown on the left. Such an operation may be analogous to the operation of the heat release zone 203 and heat exchangers 707 of the heat-exchange system 107.
  • Equations [3] and [4] can be utilized as an energy storage loop, which may reduce water consumption and can increase efficiency of the combustion system 10 by transferring heat to the feedwater intake that drive one or more turbines for generating electricity.
  • Equation [9] use of the hydration reaction shown in Equation [9] can be utilized to reduce the loss of reactivity of the sorbent material for carbon dioxide capture.

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Abstract

La présente invention porte sur des procédés et sur des systèmes de réduction des émissions de dioxyde de carbone, et selon certaines formes exécution, l'invention porte sur un four à émissions réduites de dioxyde de carbone. L'invention porte également sur des échangeurs de chaleur utilisant la chaux, la chaux délitée et la castine. L'invention porte sur des procédés visant à accroître le rendement de systèmes de combustion, et sur des procédés de capture du dioxyde de carbone provenant des systèmes de combustion afin de réduire les émissions de dioxyde de carbone.
PCT/US2006/014495 2005-04-18 2006-04-18 Procedes et systemes de reduction d'emissions Ceased WO2006113673A2 (fr)

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WO2008059378A3 (fr) * 2006-11-13 2008-10-30 Lafarge Sa Procédé de production de ciment
FR2921059A1 (fr) * 2007-09-14 2009-03-20 Rech S Geol Et Minieres Brgm E Procede et installation de production de clinker
WO2009137886A1 (fr) * 2008-05-15 2009-11-19 Calix Limited Système et procédé de traitement de gaz de carneau
DE102008050816A1 (de) * 2008-10-08 2010-04-15 Alstom Technology Ltd. Verfahren und Anordnung zur Abscheidung von CO2 aus Verbrennungsabgas
WO2011047409A1 (fr) * 2009-10-24 2011-04-28 Calix Limited Système et procédé de traitement d'un gaz combustible d'entrée et de vapeur pour la production de dioxyde de carbone et d'un gaz combustible de sortie
EP2385873A4 (fr) * 2008-11-19 2012-06-20 Univ Ohio State Res Found Procédé de réaction de carbonatation-calcination pour la capture de co2 à l'aide d'un sorbant hautement régénérable
EP2529825A1 (fr) * 2011-06-01 2012-12-05 Alstom Technology Ltd Capture de CO2 avec bouclage de carbonate
EP2559475A1 (fr) * 2011-08-15 2013-02-20 Alstom Technology Ltd. Appareil et système de capture de CO2 à partir de combustion de carburant
EP2952809A1 (fr) * 2014-06-06 2015-12-09 Alstom Technology Ltd Générateur de vapeur
US9968883B2 (en) 2014-01-17 2018-05-15 Carbonfree Chemicals Holdings, Llc Systems and methods for acid gas removal from a gaseous stream
US10583394B2 (en) 2015-02-23 2020-03-10 Carbonfree Chemicals Holdings, Llc Carbon dioxide sequestration with magnesium hydroxide and regeneration of magnesium hydroxide
WO2020201720A1 (fr) * 2019-03-29 2020-10-08 Origen Power Ltd Procédé de calcination
EP3928049B1 (fr) 2020-05-05 2022-07-27 thyssenkrupp Industrial Solutions AG Installation et procédé de fabrication de ciment pour la production de scorie de ciment
WO2023223611A1 (fr) * 2022-05-19 2023-11-23 三菱重工業株式会社 Procédé de traitement de gaz d'échappement et installation pour la mise en œuvre de ce procédé
LU103061B1 (de) 2023-01-19 2024-07-19 Thyssenkrupp Ag Energieeffiziente Abscheidung von Kohlendioxid aus einem Abgasstrom mittels eines Calciumcarbonat-Kreislaufs
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DE102023101332A1 (de) 2023-01-19 2024-07-25 Thyssenkrupp Ag Energieeffiziente Abscheidung von Kohlendioxid aus einem Abgasstrom mittels eines Calciumcarbonat-Kreislaufs
WO2024153500A1 (fr) 2023-01-19 2024-07-25 thyssenkrupp Polysius GmbH Système modulaire pour séparer, stocker et transporter du dioxyde de carbone
DE102023101316A1 (de) 2023-01-19 2024-07-25 Thyssenkrupp Ag Modulares System zur Kohlendioxidabtrennung, -lagerung und -transport
WO2024153579A1 (fr) 2023-01-19 2024-07-25 thyssenkrupp Polysius GmbH Séparation économe en énergie de dioxyde de carbone d'un flux d'échappement au moyen d'un cycle de carbonate de calcium

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WO2008059378A3 (fr) * 2006-11-13 2008-10-30 Lafarge Sa Procédé de production de ciment
US8252109B2 (en) 2006-11-13 2012-08-28 Lafarge Process for the production of cement
FR2921059A1 (fr) * 2007-09-14 2009-03-20 Rech S Geol Et Minieres Brgm E Procede et installation de production de clinker
WO2009137886A1 (fr) * 2008-05-15 2009-11-19 Calix Limited Système et procédé de traitement de gaz de carneau
US8894743B2 (en) 2008-05-15 2014-11-25 Calix Limited Method for processing flue gas
AU2009246062B2 (en) * 2008-05-15 2014-07-17 Calix Limited System and method for processing flue gas
US8632626B2 (en) 2008-05-15 2014-01-21 Calix Limited System and method for processing flue gas
DE102008050816B4 (de) * 2008-10-08 2013-09-05 Alstom Technology Ltd. Verfahren und Anordnung zur Abscheidung von CO2 aus Verbrennungsabgas
DE102008050816A1 (de) * 2008-10-08 2010-04-15 Alstom Technology Ltd. Verfahren und Anordnung zur Abscheidung von CO2 aus Verbrennungsabgas
EP2385873A4 (fr) * 2008-11-19 2012-06-20 Univ Ohio State Res Found Procédé de réaction de carbonatation-calcination pour la capture de co2 à l'aide d'un sorbant hautement régénérable
WO2011047409A1 (fr) * 2009-10-24 2011-04-28 Calix Limited Système et procédé de traitement d'un gaz combustible d'entrée et de vapeur pour la production de dioxyde de carbone et d'un gaz combustible de sortie
US9150807B2 (en) 2009-10-24 2015-10-06 Calix Limited System and method for processing an input fuel gas and steam to produce carbon dioxide and an output fuel gas
US9505998B2 (en) 2009-10-24 2016-11-29 Calix Limited System and method for processing an input fuel gas and steam to produce carbon dioxide and an output fuel gas
WO2012164370A1 (fr) * 2011-06-01 2012-12-06 Alstom Technology Ltd Capture de co2 utilisant une boucle de carbonate
EP2529825A1 (fr) * 2011-06-01 2012-12-05 Alstom Technology Ltd Capture de CO2 avec bouclage de carbonate
WO2013024339A1 (fr) * 2011-08-15 2013-02-21 Alstom Technology Ltd Appareil et système pour la capture d'émission exempte de co2 provenant de combustion de carburant
EP2559475A1 (fr) * 2011-08-15 2013-02-20 Alstom Technology Ltd. Appareil et système de capture de CO2 à partir de combustion de carburant
US9968883B2 (en) 2014-01-17 2018-05-15 Carbonfree Chemicals Holdings, Llc Systems and methods for acid gas removal from a gaseous stream
EP2952809A1 (fr) * 2014-06-06 2015-12-09 Alstom Technology Ltd Générateur de vapeur
US12179148B2 (en) 2015-02-23 2024-12-31 Carbonfree Chemicals Holdings, Llc Carbon dioxide sequestration with magnesium hydroxide and regeneration of magnesium hydroxide
US11498029B2 (en) 2015-02-23 2022-11-15 Carbonfree Chemicals Holdings, Llc Carbon dioxide sequestration with magnesium hydroxide and regeneration of magnesium hydroxide
US11772046B2 (en) 2015-02-23 2023-10-03 Carbonfree Chemicals Holdings, Llc Carbon dioxide sequestration with magnesium hydroxide and regeneration of magnesium hydroxide
US10583394B2 (en) 2015-02-23 2020-03-10 Carbonfree Chemicals Holdings, Llc Carbon dioxide sequestration with magnesium hydroxide and regeneration of magnesium hydroxide
WO2020201720A1 (fr) * 2019-03-29 2020-10-08 Origen Power Ltd Procédé de calcination
US12220692B2 (en) 2019-03-29 2025-02-11 Origen Power Ltd Calcination process
EP3928049B1 (fr) 2020-05-05 2022-07-27 thyssenkrupp Industrial Solutions AG Installation et procédé de fabrication de ciment pour la production de scorie de ciment
US12560381B2 (en) 2020-05-05 2026-02-24 thyssenkrupp Polysius GmbH Installation for the thermal treatment of dispersible raw material, and method for operating such an installation
WO2023223611A1 (fr) * 2022-05-19 2023-11-23 三菱重工業株式会社 Procédé de traitement de gaz d'échappement et installation pour la mise en œuvre de ce procédé
LU103061B1 (de) 2023-01-19 2024-07-19 Thyssenkrupp Ag Energieeffiziente Abscheidung von Kohlendioxid aus einem Abgasstrom mittels eines Calciumcarbonat-Kreislaufs
DE102023101316A1 (de) 2023-01-19 2024-07-25 Thyssenkrupp Ag Modulares System zur Kohlendioxidabtrennung, -lagerung und -transport
WO2024153579A1 (fr) 2023-01-19 2024-07-25 thyssenkrupp Polysius GmbH Séparation économe en énergie de dioxyde de carbone d'un flux d'échappement au moyen d'un cycle de carbonate de calcium
WO2024153500A1 (fr) 2023-01-19 2024-07-25 thyssenkrupp Polysius GmbH Système modulaire pour séparer, stocker et transporter du dioxyde de carbone
DE102023101332A1 (de) 2023-01-19 2024-07-25 Thyssenkrupp Ag Energieeffiziente Abscheidung von Kohlendioxid aus einem Abgasstrom mittels eines Calciumcarbonat-Kreislaufs
LU103060B1 (de) 2023-01-19 2024-07-19 Thyssenkrupp Ind Solutions Ag Modulares System zur Kohlendioxidabtrennung, -lagerung und -transport

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EP1879693A2 (fr) 2008-01-23
EP1879693A4 (fr) 2010-06-30

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