WO2006064320A1 - Procede de coproduction de charbon actif dans un procede de gazeification a lit fluidise circulant - Google Patents
Procede de coproduction de charbon actif dans un procede de gazeification a lit fluidise circulant Download PDFInfo
- Publication number
- WO2006064320A1 WO2006064320A1 PCT/IB2005/003572 IB2005003572W WO2006064320A1 WO 2006064320 A1 WO2006064320 A1 WO 2006064320A1 IB 2005003572 W IB2005003572 W IB 2005003572W WO 2006064320 A1 WO2006064320 A1 WO 2006064320A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- syngas
- solids
- activated carbon
- fluidized bed
- solids product
- Prior art date
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
- C10J3/72—Other features
- C10J3/78—High-pressure apparatus
-
- 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
- B01J20/20—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising free carbon; comprising carbon obtained by carbonising processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
- C01B32/312—Preparation
- C01B32/336—Preparation characterised by gaseous activating agents
-
- 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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- 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
- C10J2300/0956—Air or oxygen enriched air
-
- 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
- C10J2300/0969—Carbon dioxide
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
-
- 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
Definitions
- the present invention relates to a method of co-producing activated carbon in a fluidized bed gasification process, which activated carbon is especially suitable for removing mercury from the flue gases of combustion processes.
- Activated carbon is an effective adsorbent primarily due to its extensive porosity and very large available surface area. It is capable of removing low levels of organic and inorganic contaminants or impurities via transfer from the gas or liquid phase of a fluid that is being treated to the solid carbon surface of the AC. Activated carbon has been widely used to treat fluids in a large number of civil and industrial applications, such as water purification, wastewater treatment, sugar refining, beverage filtration, and air pollution control.
- AC injection is today the prevailing mercury control technology of combustion processes. Fine-grained AC is usually injected in the exhaust gases upstream of a dust collector, usually a baghouse or an electrostatic precipitator, and the spent AC is collected and disposed together with other combustion products, such as ashes. This technology has been commercialized for applications such as municipal waste and hazardous waste incinerators, and it is currently being demonstrated for application in coal-fired utility power plants. Thus, it is expected that the demand for AC will significantly increase over time.
- AC is generally produced from a wide variety of carbon-rich raw materials, including wood, coal, peat, coconut shells, nut shells, bones and fruit stones.
- the raw material, from which a given activated carbon is produced often has a substantial effect on its porosity distribution and surface area.
- activated carbons produced from different raw materials may have clearly different adsorbent qualities.
- Particle size distribution of the carbon particles is also important in AC systems because the particle size distribution influences the handling of the AC material, as well as the adsorption rates of pollutants.
- One of the methods of producing AC is a two-step process including thermal activation.
- the first step is carbonization, during which most of the volatile matter in the raw material is removed, and porous char particles are formed.
- the second step is activation by steam, during which slow and controlled oxidation further develops the porous structure of the char particles, especially so-called micropores and mesopores, and increases the total surface area.
- U.S. Patent No. 4,848,249 shows an atmospheric bubbling fluidized bed process for gasifying biomass, in which particulates containing activated carbon, with relatively low porosity, are separated from the produced combustible gas by using cyclonic separators.
- U.S. Patent No. 4,883,499 discloses a gasification process in a layered, fixed bed adapted to produce activated carbon from organic input material.
- U.S. Patent No. 5,089,030 shows a three-stage gasification apparatus and method for producing generator gas and activated carbon.
- An object of the present invention is to provide an efficient method of co- producing activated carbon from a fluidized bed gasification process.
- Another object of the present invention is to enhance the competitiveness of coal gasification by co-producing activated carbon as a valued byproduct.
- a method of co-producing activated carbon in a circulating fluidized bed gasification process comprises the steps of feeding carbonaceous fuel to a reaction chamber of a gasifier so as to form a particle bed in the reaction chamber, fluidizing the particle bed with oxygenous gas so as to partially oxidize the fuel to form syngas and char, and feeding an activation agent comprising at least one of steam and carbon dioxide to the reaction chamber so as to activate the char to form a particulate of activated carbon.
- Syngas and particulate solids entrained with the syngas from the reactor are discharged and entrained solids from the syngas are separated with a particle separator and at least a portion of the separated solids are returned through a return duct to the reaction chamber, but a solids product, comprising entrained solids of activated carbon and having an average size smaller than a predetermined size, is allowed to exit the particle separator with the syngas.
- the solids product is separated from the syngas in a dust separator, so as to form cleaned syngas.
- the cleaned syngas is discharged from the dust separator, and is supplied to a location for use in at least one of a combustion process and a chemical process.
- the solids product is discharged from the dust separator, and is supplied to a location for use in removing contaminants from a fluid.
- the method further comprises the step of utilizing the separated solids product to remove contaminants from a fluid in at least one of a water purification process, a wastewater treatment process, a sugar refining process, a beverage filtration process, and an air pollution control process. More preferably, the separated solids product is used in capturing mercury from the flue gases of a combustion process.
- the gasification of the fuel includes carbonization, during which most of the volatile matter of the fuel is removed and char particles are produced, and slow and controlled oxidation of the char particles.
- Activation of the char is realized within the gasifier system by injection of steam and/or CO 2 .
- the steam and CO2 remove carbon from the char by further oxidation through following reactions:
- the rates of the reactions are strictly controlled to maximize the internal surface area of the char. Both reactions are endothermic and supported with energy from the thermal energy of the circulating bed material originating from controlled oxidation of char and volatile matter.
- Steam and/or CO 2 may be injected into the bottom of the reaction chamber of the gasifier premixed with oxygenous fluidizing gas (preferably air). Additionally or alternatively, steam and/or CO 2 may be introduced into higher elevations in the reaction chamber through a sidewall of the chamber, or to a fluidized bed formed in the return duct.
- the gasifier is operated at an elevated pressure.
- the gasifier is operated at a pressure suitable for combusting the produced syngas in a gas turbine combustor, preferably at a pressure from about 10 bar to about 20 bar.
- the syngas is combusted in an atmospheric combustor (e.g., in a utility boiler), and the gasifier can be operated at, or close to, atmospheric pressure. It is also possible to utilize the syngas in a chemical process (e.g., in producing hydrogen, ammonia, liquid fuels or fine chemicals).
- a circulating fluidized bed gasifier the fuel is circulating for an extended time from the reactor to the particle separator and via the return duct back to the reactor.
- the total residence time of the fuel in the fluidized bed and, consequently, the time being affected by the activating agent is long enough to impart a highly porous structure to the char particles, so as to produce activated carbon in the solids product.
- a circulating fluidized bed gasifier provides a relatively uniform and controllable temperature, so that the activation process of the char can be optimized to provide a desired pore structure to the produced activated carbon.
- the activation agent is effectively mixed with the char in the strongly turbulent bed of particles, and causes efficient activation of the char.
- the present method is especially advantageous when using bituminous or subbituminous coal or lignite as fuel. It has been observed that, when using subbituminous coal, activation in the fluidized bed in the reaction chamber is usually sufficient to produce activated carbon applicable to air pollution control applications, especially for reducing mercury from the flue gas of a combustion process. However, especially when the fuel is bituminous coal, it has been found to be beneficial to add a further step of activating the char with at least one of steam and carbon dioxide in a fluidized activation chamber arranged in a hot loop of the circulating fluidized bed gasifier. In some cases, such an activation chamber may be needed for subbituminous coals and lignite, as well.
- the average activation time for the char is at least twenty (20) minutes; even more preferably, at least forty (40) minutes.
- the average activation time is preferably at least about sixty (60) minutes.
- the activated carbon produced in a process in accordance with the present invention, has sufficient activity for applications such as air pollution control and wastewater treatment when the adsorbent is used once and then disposed of.
- the activated carbon product from this process may be further enhanced or modified by one or more conventional chemical processes, such as sulfur impregnation.
- FIG. 1 is a schematic view of a circulating fluidized bed gasifier in accordance with the present invention. DESCRIPTION OF THE PREFERRED EMBODIMENTS
- FIG. 1 schematically illustrates a circulating fluidized bed (CFB) gasifier 10 which can be used in a preferred embodiment of a gasification process in accordance with the present invention.
- the CFB gasifier 10 comprises a reaction chamber 12 with a fuel supply 14 for feeding carbonaceous fuel to a particle bed formed in the reaction chamber 12.
- the chamber 12 also comprises an oxidizing gas supply 16 for feeding oxidizing gas (usually air), and an activating agent supply 18 for feeding activation agent, steam, and/or carbon dioxide, at controlled rates into the reaction chamber 12.
- the activation agent supply 18 may be fed to the reaction chamber 12 through the bottom grid 20, possibly premixed with the oxidizing gas (the lower instance of activation agent supply 18 in Fig. 1), and/or at higher elevations through a side wall 22 of the reaction chamber 12 (the upper instance of activation agent supply 18 in Fig. 1).
- the fuel and other particulate solids in the bed are fluidized in a conventional way with less than stoichiometric oxygen present, causing gasification of the fuel to syngas and char.
- the char is further activated with the activation agent, the porosity of the char is highly enhanced and activated carbon is formed.
- a turbulent fluidized state of the bed creates a nearly isothermal temperature zone with high thermal inertia, and enables accurate control of the reaction temperature.
- the reaction chamber 12 is advantageously operated at a predetermined temperature, preferably at a temperature between about 500 °C and about 1100 °C.
- the temperature can, at least to a certain extent, be optimized for rapid activation so as to produce activated carbon with a desired porous structure.
- the operating temperature range of the reaction chamber 12 is from about 800 0 C to about 1000 0 C.
- the superficial fluidizing velocity in the reaction chamber 12 is preferably from about 1.5 m/s to about 9 m/s, even more preferably from about 3 m/s to about 6 m/s.
- the produced syngas carries solid particles vertically up through the reaction chamber 12.
- the syngas and solids entrained with the syngas are discharged through an outlet 24 in the upper portion of the reaction chamber 12 to a particle separator 26.
- Most of the solids entrained in the syngas are separated from the syngas in the particle separator 26 (preferably, a cyclone separator) to be returned via a return duct 28 to the lower portion of the reaction chamber 12.
- the finest portion of the entrained solids, comprising mainly activated carbon, is discharged from the particle separator 26, together with the syngas, through a gas outlet 30 to a syngas line 32.
- the syngas is cooled by a syngas cooler 34 arranged in the syngas line 32.
- the remaining fine particles are separated from the syngas in a dust separator 36 (preferably, a barrier filter).
- the cleaned syngas is discharged from the dust separator 36 through a gas discharge line 38 to a combustion process (e.g., to drive a gas turbine generator), or to a chemical process (e.g., to produce high value products such as hydrogen, ammonia, liquid fuels or fine chemicals).
- the solids product which comprises mainly fine activated carbon particles separated from the syngas in the dust separator 36, is discharged from the dust separator 36 through a solids discharge line 40, to be used in a suitable application, such as in capturing emissions (especially mercury) from a combustion process, or in wastewater treatment.
- Coarse char accumulating at the bottom of the reaction chamber 12 is drained therefrom through a bottom outlet 42. It may be useful in some applications to grind the drained coarse char to a desirable particle size, and mix it with the solids product discharged from the dust separator 36 through the solids discharge line 40.
- the particle size of the solids product can to some extent be controlled by adjusting the particle size of the raw material fed to the reactor chamber. However, significant size reduction occurs in the CFB gasifier due to fragmentation and attrition.
- the particle separator 26 works as a classifier that mainly allows only particles smaller than a certain size to exit the separator with the syngas.
- the particle size of the solids product can be controlled by controlling the separation efficiency of the separator 26.
- the separation efficiency of the particle separator 26 is such that the average particle size of the particles discharged from the separator with the syngas is less than about 60 ⁇ m, even more preferentially less than about 45 ⁇ m.
- the gasifier 10 is operated at an elevated pressure.
- the pressure in the reaction chamber 12 is from about 2 bar to about 70 bar, even more preferably from about 10 bar to about 20 bar.
- the reaction chamber is usually enclosed in a pressure vessel and the fuel feed means and solids removal means are equipped with means for pressure adjustment. These are, however, not shown in FIG. 1.
- the process described above can be used to produce activated carbon from many raw materials, including various ranks of coals and various types of biomass. It has been observed that activating char in the reactor of a circulating fluidized bed gasifier is usually sufficient for subbituminous coal, but not for bituminous coal. Therefore, especially when gasifying bituminous coal, a fluidized activation chamber 44 is advantageously arranged to the return duct 28 of the gasifier 10, so as to extend the total activation time of the carbon in the ashes.
- the bed formed in the activation chamber 44 is preferably fluidized, by using a fluidizing agent supply 46 with the activation agent, steam, and/or carbon dioxide.
- the fluidizing agent from the fluidizing agent supply 46 may be mixed with some oxygenous gas (preferably air), so as to effect some oxidation of the char, for maintaining the activation chamber 44 at a desired temperature, preferably above about 800 °C.
- the total effective activation time of the carbon is preferably extended to about one (1) hour, or even higher.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Industrial Gases (AREA)
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Abstract
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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US11/012,289 | 2004-12-16 | ||
US11/012,289 US20060130401A1 (en) | 2004-12-16 | 2004-12-16 | Method of co-producing activated carbon in a circulating fluidized bed gasification process |
Publications (1)
Publication Number | Publication Date |
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WO2006064320A1 true WO2006064320A1 (fr) | 2006-06-22 |
Family
ID=35705325
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/IB2005/003572 WO2006064320A1 (fr) | 2004-12-16 | 2005-11-29 | Procede de coproduction de charbon actif dans un procede de gazeification a lit fluidise circulant |
Country Status (2)
Country | Link |
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US (1) | US20060130401A1 (fr) |
WO (1) | WO2006064320A1 (fr) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2147965A1 (fr) * | 2007-05-14 | 2010-01-27 | Keda Industrial Co., Ltd. | Système de four de génération de gaz de houille à lit fluidisé et circulation de charbon |
WO2010015316A2 (fr) * | 2008-08-05 | 2010-02-11 | Krones Ag | Procédé et dispositif de production de gaz de synthèse à partir de biomasse |
EP2284245A1 (fr) * | 1997-12-09 | 2011-02-16 | DONG Energy Power A/S | Réacteur à lit fluidisé avec séparateur de particules et chambre de reaction. |
CN101372635B (zh) * | 2008-10-15 | 2011-07-06 | 东南大学 | 高密度增压流化床煤气化装置及方法 |
CN103409168A (zh) * | 2013-08-08 | 2013-11-27 | 大连理工大学 | 一种煤气化快速联产活性炭的方法 |
US8637209B2 (en) | 2005-08-09 | 2014-01-28 | Allan J. Jacobson | Cathode and electrolyte materials for solid oxide fuel cells and ion transport membranes |
US9236615B2 (en) | 2005-08-09 | 2016-01-12 | The University Of Houston System | Methods for using novel cathode and electrolyte materials for solid oxide fuel cells and ion transport membranes |
CN106675658A (zh) * | 2016-12-15 | 2017-05-17 | 华北电力大学 | 一种高通量循环流化床低阶煤气化装置及方法 |
US9688934B2 (en) | 2007-11-23 | 2017-06-27 | Bixby Energy Systems, Inc. | Process for and processor of natural gas and activated carbon together with blower |
WO2020148551A3 (fr) * | 2019-01-17 | 2020-09-03 | Rifat Al Chalabi | Procédé pour produire du charbon actif et de l'hydrogène |
RU2777640C1 (ru) * | 2022-02-03 | 2022-08-08 | Петр Александрович Левин | Способ получения углеродного сорбента в кипящем слое |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20090232725A1 (en) | 2007-11-23 | 2009-09-17 | Sherman Aaron | Flow rate of gas in fluidized bed during conversion of carbon based material to natural gas and activated carbon |
FR2955854B1 (fr) | 2010-02-01 | 2014-08-08 | Cotaver | Procede et systeme de production d'hydrogene a partir de matiere premiere carbonee |
FR2955865B1 (fr) | 2010-02-01 | 2012-03-16 | Cotaver | Procede de recyclage du dioxyde de carbone (co2) |
FR2955918B1 (fr) * | 2010-02-01 | 2012-08-03 | Cotaver | Procede et systeme de production d'une source d'energie thermodynamique par la conversion de co2 sur des matieres premieres carbonees |
FR2955866B1 (fr) | 2010-02-01 | 2013-03-22 | Cotaver | Procede et systeme d'approvisionnement en energie thermique d'un systeme de traitement thermique et installation mettant en oeuvre un tel systeme |
US20110197797A1 (en) * | 2010-02-18 | 2011-08-18 | Chavond-Barry Engineering Corp. | Method and apparatus for efficient production of activated carbon |
FR2986800B1 (fr) | 2012-02-09 | 2015-01-30 | Cotaver | Procede, systeme et installation de traitement de matieres hydrocarbonees liquides et/ou pateuses |
NL2019553B1 (en) * | 2017-09-14 | 2019-03-27 | Torrgas Tech B V | Process to prepare an activated carbon product and a syngas mixture |
CN109305681B (zh) * | 2018-11-30 | 2022-02-08 | 南通滨海活性炭有限公司 | 危废活性炭及生物质材料制造活性炭的工艺 |
CN112824502B (zh) * | 2019-11-21 | 2022-04-15 | 中国科学院工程热物理研究所 | 循环流化床气化装置以及循环流化床气化方法 |
US11834338B1 (en) | 2022-05-24 | 2023-12-05 | John W. Black | Continuous carbonaceous matter thermolysis and pressurized char activation with hydrogen production |
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US5672323A (en) * | 1995-01-26 | 1997-09-30 | The Babcock & Wilcox Company | Activated carbon flue gas desulfurization systems for mercury removal |
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2004
- 2004-12-16 US US11/012,289 patent/US20060130401A1/en not_active Abandoned
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2005
- 2005-11-29 WO PCT/IB2005/003572 patent/WO2006064320A1/fr active Application Filing
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US3677727A (en) * | 1970-08-14 | 1972-07-18 | Activit Sa | Process of activation and gasification of fluidised carbonaceous materials |
US4002533A (en) * | 1972-07-06 | 1977-01-11 | Westvaco Corporation | Two-step process for conditioning sized coal and resulting product |
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GB2596020A (en) * | 2019-01-17 | 2021-12-15 | Al Chalabi Rifat | Process for producing activated carbon and hydrogen |
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