US20110078951A1 - Two-stage high-temperature preheated steam gasifier - Google Patents

Two-stage high-temperature preheated steam gasifier Download PDF

Info

Publication number
US20110078951A1
US20110078951A1 US12/994,907 US99490709A US2011078951A1 US 20110078951 A1 US20110078951 A1 US 20110078951A1 US 99490709 A US99490709 A US 99490709A US 2011078951 A1 US2011078951 A1 US 2011078951A1
Authority
US
United States
Prior art keywords
reactor
gasifier
temperature
steam
stage
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US12/994,907
Other languages
English (en)
Inventor
Wlodzimierz Blasiak
Weihong Yang
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Boson Energy SA
Original Assignee
Boson Energy SA
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Boson Energy SA filed Critical Boson Energy SA
Publication of US20110078951A1 publication Critical patent/US20110078951A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • C10J3/14—Continuous processes using gaseous heat-carriers
    • 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
    • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
    • 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
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/36—Fixed grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/094—Char
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0973—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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the present invention generally relates to a two-stage high-temperature steam gasifier for producing synthesis gas and, optionally, activated carbon, from a coarse carbonaceous feedstock, and more particularly to a gasifier capable of simultaneously gasifying a coarse solid carbonaceous feedstock and a fine solid carbonaceous feedstock or a liquid carbonaceous feedstock.
  • the present invention also relates to a process of gasifying a coarse carbonaceous feedstock using a two-stage gasifier having two reactors in order to produce synthesis gas, optionally together with activated carbon, wherein no oxygen is fed to the first stage reactor, but only preheated steam having a temperature of at least 700° C.
  • Gasification is a high-temperature thermal decomposition process of converting a solid feedstock, such as solid coal, petroleum coke, biomass, and/or solid waste, a liquid feedstock, such as black liquid oil, or a gaseous feedstock, into a fuel gas, consisting primarily of hydrogen (H 2 ) and carbon monoxide (CO), with lesser amounts of carbon dioxide (CO 2 ), water (H 2 O), methane (CH 4 ), higher hydrocarbons, and nitrogen (N 2 ) using reactants such as air, steam, and oxygen, either alone or in any combination thereof.
  • a solid feedstock such as solid coal, petroleum coke, biomass, and/or solid waste
  • a liquid feedstock such as black liquid oil, or a gaseous feedstock
  • a fuel gas consisting primarily of hydrogen (H 2 ) and carbon monoxide (CO), with lesser amounts of carbon dioxide (CO 2 ), water (H 2 O), methane (CH 4 ), higher hydrocarbons, and nitrogen (N 2 ) using reactants such as
  • the thermal gasification processes are highly endothermic chemical reactions.
  • the general methods for supplying heat for the gasification use either of the following: a) an external source, e.g. sensible heat from hot char recirculation, and/or sensible heat from a heated gasification agent, b) reaction heat from oxidization of a part of the feedstock (incoming carbonaceous materials), and c) exothermal reaction heat from a non-carbonaceous material such as calcined lime and CO 2 .
  • US 2004/0060236 A1 teaches an economic small scale gasification system for gasifying solid fuel into pyrolysis gas, wherein heated mixed gas of steam and air is introduced into a reformer along with the pyrolysis gas producing reformed high temperature crude gas.
  • the mixed gas of air and steam is preferably heated to at least 300° C., and more preferably at least 400° C. Any type of heat exchanger or heater may be employed as the air/steam heating device for heating the mixed gas of air and steam.
  • U.S. Pat. No. 6,837,910 teaches an apparatus and method for gasifying liquid or solid fuel, wherein a heated mixed gas of steam and air is introduced into at least one of the thermal decomposition area of the solid or liquid fuel and the reforming area of the thermal decomposed gas.
  • the mixed gas of air and steam is heated to a temperature of at least 700° C., and more preferably higher than 800° C.
  • a method for gasifying carbonaceous materials into fuel gases involves the formation of an ultra-superheated steam (USS) composition substantially containing water vapor, carbon dioxide and highly reactive free radicals thereof, at a temperature of about 1316° C. to about 2760° C.
  • USS ultra-superheated steam
  • the USS composition comprising a high temperature flame is contacted with a carbonaceous material for rapid gasification/reforming thereof.
  • the USS is formed by burning s substantially ash-free fuel with “artificial air” comprising an enhanced oxygen gas and water vapour, wherein the “artificial air” is at least about 60 mole percent.
  • the oxygen:fuel ratio will have to be controlled so that soot is not is not formed.
  • the use of enhanced oxygen gas in the method will obviously increase the operation cost of the method.
  • thermal conversion of biomass/waste/coal can be understood as comprising two mainly highly endothermic stages: devolatilization of volatiles, and char conversion, respectively.
  • devolatilization of volatiles 90% of the volatile content in the total weight of biomass will be released instantaneously if it would be heated above 600° C.
  • the second stage is char conversion.
  • a much higher temperature is needed for the thermal conversion of char. Generally, this temperature should be higher than 1000° C., depending on the ash melting point.
  • Nary et al. Biomass gasification with air in an atmospheric bubbling fluidized bed. Effect of six operational variables on the quality of produced raw gas, Industrial and Engineering Chemistry Research 35 (1996) (7), pp. 2110-2120) performed secondary air injection in the freeboard of a fluidized bed gasifier and observed a temperature rise of about 70° C. which resulted in a tar reduction from 28 to 16 g/Nm 3 .
  • the Asian Institute of Technology (AIT), Thailand, modified a biomass gasifier which resulted in a fuel gas with a tar production of about 50 mg/Nm 3 , which is about 40 times less than a single-stage reactor under similar operating conditions (T. A. Milne and R. J. Evans, Biomass Gasification “Tars”: Their Nature, Formation and Conversion. NREL, Golden, Colo., USA, Report No. NREL/TP-570-25357 (1998).
  • This concept involves a downdraft gasifier with two levels of air intakes.
  • the produced tar in the biomass pyrolysis process will pass through a high-temperature residue char bed at the bottom and will be decomposed at the elevated temperature.
  • U.S. Pat. No. 6,960,234 discloses a multi-faceted gasifier and related methods. It is a gasifier combing a fixed bed gasification section and an entrained flow gasification section. Activated carbon may be formed in the upper fixed bed section and in the entrained flow section.
  • U.S. Pat. No. 6,647,903 discloses a method and apparatus for generating and utilizing combustible gas using a gasifier comprising first and second reaction sections, wherein oxidizing gas is introduced into both sections.
  • the invention operates in a manner that enhances tar destruction while forming output fuel gas products H 2 and CO.
  • some methane may also be formed.
  • activated carbon may be generated.
  • JP 6256775 discloses two-stage complete gasification of organic matter for methane synthesis, wherein in a first stage gasification process organic matter is gasified in the presence of steam and oxygen, and, in a second stage gasification process gaseous un-reacted matter and tar gas are gasified at a higher temperature than in the first stage gasification process.
  • a gasifier comprising two stages is also disclosed. In order to disturb solid carbonaceous material from passing from the first stage gasification process to the second stage gasification process, the passage between the two stages may be narrowed, or a filter may be set between the two stages.
  • the gasifier includes two inlets for oxygen and steam, one in the first stage, and the other in the second stage.
  • the aim of secondary air/oxygen and/fuel injection in above works is increasing the temperature in freeboard in order to decompose tar, and improve the steam-reform reaction.
  • the injection of secondary air will not only increases the diluents contents, notably nitrogen, but will also reduce the combustible contents generated from gasification. This results in a decrease of LCV of the fuel gas produced.
  • injection of secondary air makes it hard to control the composition of the produce gas.
  • a novel fixed bed gasifier is proposed herein.
  • Such gasifier is specified in claim 1 .
  • a method of gasifying a coarse carbonaceous feedstock, using a two-staged gasifier having two reactors, in order to produce synthesis gas, optionally together with activated carbon, wherein no oxygen is fed to the first stage reactor, but only preheated steam having a temperature of at least 700° C. is also claimed and disclosed. Such method is provided for in claim 4 .
  • a two-stage gasifier of the prior art comprising: a first reactor provided with an inlet for a coarse carbonaceous feedstock, and a first inlet for steam; and a second reactor provided with a second inlet for steam, optionally together with air or oxygen; and an outlet for synthesis gas; wherein the first and second reactors are separated by a narrowed portion having a reduced cross-section for restricting passage from the first reactor to the second reactor of unreacted solid carbonaceous substance, wherein the first reactor is capable of being operated at a temperature of at least 600° C., and wherein the second reactor is capable of being operated at a higher temperature, the above object has been achieved by means of the technical features of the characterizing portion of said claim, according to which the second reactor is the lower reactor, the first reactor is the upper reactor, a grate is provided at the bottom end of the first reactor, said first inlet for steam is located adjacent to the bottom of the first re
  • said first reactor is provided with an outlet for synthesis gas
  • the second reactor is provided with an inlet for a fine solid carbonaceous feedstock and/or a liquid carbonaceous feedstock
  • said second inlet for steam is located adjacent to the bottom of the second rector, so as to enable preheated steam having a temperature of at least 700° C., optionally together with preheated air or oxygen of same temperature, to be fed to the second reactor from below via said inlet, and a second narrowed portion having a reduced cross-section is provided at the bottom end of the second reactor.
  • the present invention relates to a two-stage gasifier as set out above.
  • gasifier of the invention simultaneous gasification of solid coarse material, on the one hand, and solid fine and/or liquid material, on the other, is enabled.
  • Carbonaceous coarse material is fed to the first reactor and carbonaceous (waste) liquid and/or carbonaceous fine solid material is fed to the second reactor.
  • one or more, and preferably all of the inlets for steam, air, oxygen and carbonaceous (waste) liquid and/or carbonaceous fine solid material enter into the gasifier tangentially in corresponding portions of the gasifier, which portions have an inner, circular cross-sections.
  • the inlet for carbonaceous (waste) liquid and/or carbonaceous fine solid material comprises at least two inlets separated at a maximum distance from each other along the circumference of the circular cross-section.
  • the present invention relates to a process of gasifying a coarse carbonaceous feedstock, using a two-stage gasifier having two reactors, a first and a second, respectively, in order to produce synthesis gas, optionally together with activated carbon.
  • a process of gasifying a coarse carbonaceous feedstock using a two-stage gasifier having two reactors, a first and a second, respectively, in order to produce synthesis gas, optionally together with activated carbon.
  • Such process is provided for in claim 4 , and includes the following steps: (a) feeding a coarse carbonaceous feedstock to the first stage reactor of the gasifier; (b) subjecting the coarse carbonaceous feedstock to steam in the first stage reactor at an operational temperature of at least 600° C.
  • step (c) wherein any solid and/or liquid carbonaceous materials obtained from step (b) are subjected to preheated steam, optionally together with air or oxygen, in the second stage reactor operating at a temperature of at least 700° C. to obtain any combination of the following products: activated carbon; CO; CO 2 , and heat of combustion.
  • the process comprises a further step (d) wherein a fine solid carbonaceous, and/or liquid carbonaceous feedstock, is/are being fed simultaneously into the second stage reactor of the gasifier. Accordingly, in this embodiment both a coarse feedstock and a fine solid and/or liquid carbonaceous feedstock may be fed simultaneously into the gasifier.
  • externally generated preheated steam having a temperature of at least 700° C. is also fed into the second stage reactor.
  • internal combustion also referred to as partial combustion or oxidation
  • in the gasifier can be kept to a minimum, since the required energy is provided externally. Consequently, supply of air or oxygen is not required for heat generation by internal combustion in this embodiment. Also, when air or oxygen is not being fed to the second reactor the yield of activated carbon can be maximised.
  • air is fed to the second reactor (i.e. in addition to the high temperature steam).
  • air is fed to the second reactor (i.e. in addition to the high temperature steam).
  • FIG. 1 shows a system flow diagram generally illustrating the inventive gasification process for biomass and solid waste.
  • FIG. 2 illustrates a cross-sectional view of an embodiment of the gasifier 21 .
  • FIG. 3 is a plan view of the inventive gasifier showing the tangential liquid feedstock injection via inlets 19 a and 19 b.
  • the inventive gasifier combines two reactors using externally generated preheated high temperature steam injection into the first reactor, where the heating demand for gasification is supplied by the sensible energy from the steam.
  • the gasifier can produce a medium and higher LCV syngas.
  • the first reactor is a fixed bed gasification section where the coarse feedstock is gasified
  • the second reactor is an entrained-bed gasification section where the liquid and fine feedstock is gasified.
  • Solid coarse feedstock is devolatilized in the first fixed bed reactor of the gasifier by means of high-temperature steam, and subsequently, in the second reactor subjected to a higher temperature sufficient to crack and destroy tars and oils.
  • Activated carbon may be formed as co-product.
  • the gasifier may be used with various solid and liquid feedstocks.
  • the gasifier is capable of gasifying such different feedstocks simultaneously.
  • the idea behind the present invention is that the gasifier 21 is separated into two stages: a first upper stage 3 for devolatilization of volatiles, which first stage only uses externally generated high-temperature preheated pure steam (preferably 700° C.-1000° C.), and a second lower stage 4 for char thermal conversion, using a high-temperature (preferably 700-1600° C., more preferably 800-1200° C.) preheated mixture of air and steam, oxygen and steam, or steam only as shown in FIG. 1 .
  • the reactor 3 includes a fixed bed comprising grate 8 .
  • the energy used for the devolatilization process is supplied both by the sensible energy of steam fed into the first reactor via inlet 7 , and by the hot stream coming from the second reactor through the narrowed portion 20 .
  • the temperature in the first reactor is controlled at the level of at least 600° C. by the quantity and the temperature of the steam fed into said reactor.
  • a little oxygen released from the pyrolysis (which occurs in the first reactor, and also in the second reactor when a liquid and/or solid fine feedstock is being injected) and from the second reactor 4 reacts according to the following:
  • any solid and/or liquid char produced in the first reactor will not be reacted with any oxidizers in said reactor. Consequently, any solid and/or liquid char will instead fall into the second reactor 4 by the action of the gravity.
  • the energy used for char the conversion process is preferably supplied by the sensible energy of mixture of steam and air, and from partial oxidization of char.
  • the temperature in the second reactor should be higher than that of the ash melting point, in order for the ash to form slag. Normally, for wood biomass the ash melting point can be 1300° C.
  • the reactor 4 includes an entrained bed comprising grate 5 .
  • the activated carbon can be treated as a co-production from thermal conversion of carbon-based materials through this invention.
  • the preparation of activated carbon involves two steps: carbonization of the raw material in absence of oxygen at high temperature (500-1000° C.) in order to eliminate maximum amounts of oxygen and hydrogen elements, and activation of the carbonized product at a higher temperature in the presence of oxidizing gas such as water, carbon dioxide or both.
  • the activation shall be carried out under well controlled conditions in order to achieve a desired conversion.
  • the feedstock is first gasified by high-temperature pure steam (at the level of at least 600° C.) in the first reactor 3 , then the carbon is preferably activated in the second reactor 4 by high-temperature steam.
  • high temperature steam and optionally air or oxygen (over 700° C.)
  • air or oxygen over 700° C.
  • FIG. 2 illustrates a cross-sectional view of the gasifier 21 .
  • Carbonaceous feedstock 1 enters at the top of the gasifier, through a feed inlet 2 , and proceeds downward moving through the first reactor 3 , then pass the grate 8 , then enters second reactor 4 , then pass the grate 5 until it becomes a molten ash at the bottom 6 .
  • the feedstock can include biomass, coal, municipal solid waste, or any combination thereof.
  • the particle size of the coarse carbonaceous feedstock 1 is typically from 0.5 cm to 1.8 cm, and preferably from 0.5 to 1.2 cm.
  • the feedstock is heated by a combination of the sensible heat carried by the high-temperature steam (over 700° C.), and the sensible heat carried by the flue gas produced by char oxidization and gasification in the second reactor 4 .
  • High-temperature steam carried by pipe 7 for the feedstock gasification in the first reactor enters a narrowed portion or throat 20 through a port (ports) 11 .
  • the amount of high-temperature steam added at port 7 is set to keep the temperature at point 3 (first reactor) between 600-900° C., and preferably above 700° C.
  • the temperature in the reactor 3 is controlled by the temperature and flowrate of injection of steam from point 7 , and the temperature and quantity of surplus oxygen from reactor 4 .
  • the residence time of the feedstock 1 inside reactor 3 is mainly controlled by the gap of the grate 8 .
  • a throat 20 is provided.
  • the diameter of the throat is generally smaller than that of the hearth of reactor 3 .
  • the inclination of the conical portion 14 should preferably be around 45-60°.
  • the diameter of the steam injection port 11 should preferably be 2-3 times smaller than that of the throat 20 .
  • the remaining fixed carbon has become activated carbon char and ash solids, which continue to move downward through the grate 8 , then enter a throat 20 , then enter into the second reactor 4 , where they are oxidized and gasified by a mixture of high-temperature air (or oxygen) and steam.
  • a mixture of high-temperature air (or oxygen) and steam When no air or oxygen is being fed with the steam into reactor 4 , no oxidation will occur in reactor 4 , but only gasification.
  • the temperature of the second reactor 4 is further increased to a temperature slightly above the ash softening point of the fuel at the grate 5 .
  • the pipe 9 carries the preheated high-temperature steam or mixture of high-temperature air (or oxygen) and steam to the port 10 , which then enters into the second throat 18 .
  • the ash softening point typically ranges from 1350-1400° C. If slag formation of the ash is to be avoided, the maximum peak temperature in the reactor 4 during operation is maintained at a temperature at least 50° C. below the ash softening point, with 100° C. below as the normal and thus preferred maximum condition.
  • the temperature in reactor 4 is controlled by the preheating temperature, flowrate and the ratio of steam to carbon, and, when air or oxygen also is being used with the steam, the ratio of steam to oxygen of the mixture.
  • the diameter of the second narrowed portion or throat 18 is generally smaller than that of the diameter of reactor 4 , and preferably also smaller than that of the first narrowed portion or throat 20 .
  • the inclination of the conical portion 17 should preferably be around 45-60°.
  • the diameter of the steam injection port 10 should preferably be 3-5 times smaller than that of the throat 18 .
  • the ash is dropped into bottom 6 through throat 18 , and may be taken out batch-wise from the reactor.
  • syngas flows out through the exit pipe 12 . Since the temperature in the first reactor 3 is high enough, and also steam is present, most of the tar is destroyed and converted to syngas.
  • the main chemical constituents of syngas are hydrogen, carbon monoxide, and methane, and carbon dioxide.
  • the inventive design of the gasifier has the ability to advantageously control the ratio of hydrogen to carbon monoxide in the syngas, since the gasifier enables control within wide ranges of steam to oxygen ratio within the gasifier.
  • the second reactor 4 by controlling the temperature in the second reactor 4 at 700° C., i.e. the same temperature as first reactor 3 , and by only feeding steam to the second reactor, all tars and oils are consumed by the high-temperature steam. This converts most of the fixed-carbon to activated carbon within the gasifier. Therefore, the gasifier and process described herein can also effectively generate activated carbon. This mode of operation is very effective for generating activated carbon, and will also improve the quality of the activated carbon obtained. If gasification is to be maximized, on the other hand, the second reactor should be operated at a higher temperature than the first reactor.
  • the invention can consequently also be used to produce activated carbon.
  • activated carbon is created within the gasifier.
  • first one only the first reactor is used, i.e. only high-temperature steam is injected through pipe 7 .
  • the high-temperature mixture of steam and air from pipe 9 is closed.
  • Another and more preferred method is to have both reactors running, but from pipe 9 , only high-temperature steam is injected.
  • the activated carbon is collected into dry directly.
  • the second method has surprisingly been found to be apt to give higher quality of the activated carbon char. This is believed to be due to that the high-temperature steam injected from pipe 9 makes the pores of the activated carbon opening in the second reactor 4 .
  • Activated carbon having wider pores than in the prior art may thus be obtained by means of the method of the invention.
  • the size (diameter of pores) can be controlled by the temperature of steam in the reactor 4 . Generally, a higher temperature of steam increases the pore number of the activated carbon.
  • the present invention is capable of achieving a bi-generation (gas and activated carbon) from one and the same feedstock 1 .
  • the desired ratio of the products can be decided upon according to the type of feedstock available, price of the products, and so on.
  • this invention can be used to treat both coarse particles (diameter larger than 0.5 cm) of carbonaceous materials and fine particles and or liquid feedstock.
  • FIG. 3 shows a cross-sectional view of the gasifier 21 , which shows the tangential liquid/fine particles feedstock injection.
  • Two injection lances 19 ( 19 a and 19 b ) are shown connecting to the reactor 4 .
  • Liquid feedstock such as the liquid residues collected after a micro-oven pyrolysis process of the Automotive Shredder Residue (ASR), and fine or pulverized feedstock can be injected into the reactor 4 .
  • the injected feedstock enters into the reactor 4 tangentially and mixes with the high-temperature air/steam coming from the grate 5 .
  • the tangential injection can increase the residence time of the liquid and/or fine feedstock.
  • the entrained flow gases pass through the upper fixed bed grate 8 , then enter reactor 3 before leaving the gasifier at the exit pipe 12 .
  • the injection port 19 should be located to the lower part of the hearth of the reactor 4 in order to increase the residence time. Generally, for a small-scale gasifier, the location of this injection port(s) is 10 cm above the inclination wall 17 .
  • the residue time can be controlled by the injection velocity, and the angle of the injection lance to the gasifier.
  • the walls of the gasifier consist of two layers: an outer steel cover, preferably 5.0 mm thick, and an inner layer of fibrous ceramic insulation, preferably a high temperature resistant, high quality ceramic.
  • the ceramic used at walls 13 and 14 can preferably operate with, i.e. withstand, a maximum temperature of 1400° C.
  • a suitable material may be composed of: Al 2 O 3 45%, SiO 2 36%, Fe 2 O 3 , 0.9% and CaO 16%.
  • the ceramic used for the walls at 15 , 16 and 17 is preferably apt to operate at a higher temperature of 1400-1500° C.
  • the maximum allowed working temperature of this wall material is 1600° C.
  • a suitable material may have the following composition: Al 2 O 3 61%, SiO 2 26%, Fe 2 O 3 , 0.5%, CaO 2.6%, ZrO2 2.95%, and BaO 3.3%.
  • the ceramic materials are supported by a steel shell.
  • refractive ceramic tubes are used as the grates 8 and 5 .
  • the composition of these ceramic tubes can for example be 97% ZrO 2 , and 3% of MgO.
  • a high temperature mixture of steam, optionally together with air or oxygen, being fed through pipe 9 enters the throat 18 which below the grate 5 .
  • This high temperature mixture of air and steam can keep the ash in a molten state in the throat 18 , which ash finally drops to the bottom 6 , and can be taken out in batches.
  • Wood Pellets Total Moisture (SS187170) 8% Ash content (SS-187171) 0.5-0.6% (dry) LHV (SS-ISO562) 17.76 MJ/kg (as received) Volatile matter (SS-ISO) 84% (dry) Density 630-650 kg/m 3 Ultimate analysis (dry compositions) Wood Pellets Sulphur (SS-187177) S 0.01-0.02% Carbon (Leco-600) C 50% Hydrogen (Leco-600) H 6.0-6.2% Nitrogen (Leco-600) N ⁇ 0.1% Oxygen (Calculated) O 43-44% Ash fusion temperatures (oxidizing conditions) Wood Pellets Initial deformation, IT 1350-1400° C. Softening, ST 1450-1500° C. Hemispherical, HT 1500° C. Fluid temperature, FT 1500-1550° C.
  • RDF Refuse Derived Fuel

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US12/994,907 2008-05-29 2009-05-29 Two-stage high-temperature preheated steam gasifier Abandoned US20110078951A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
SE0801266A SE0801266A0 (sv) 2008-05-29 2008-05-29 Tvåstegsförgasare som använder förupphettad ånga av hög temperatur
SE0801266-8 2008-05-29
PCT/SE2009/050630 WO2009145724A2 (en) 2008-05-29 2009-05-29 A two-stage high-temperature preheated steam gasifier

Publications (1)

Publication Number Publication Date
US20110078951A1 true US20110078951A1 (en) 2011-04-07

Family

ID=41377827

Family Applications (1)

Application Number Title Priority Date Filing Date
US12/994,907 Abandoned US20110078951A1 (en) 2008-05-29 2009-05-29 Two-stage high-temperature preheated steam gasifier

Country Status (12)

Country Link
US (1) US20110078951A1 (xx)
EP (1) EP2300568A2 (xx)
JP (1) JP2011522084A (xx)
CN (1) CN102076830A (xx)
AP (1) AP2010005514A0 (xx)
AU (1) AU2009251931A1 (xx)
BR (1) BRPI0912280A2 (xx)
CA (1) CA2726250A1 (xx)
EA (1) EA017739B1 (xx)
SE (2) SE0801266A0 (xx)
WO (1) WO2009145724A2 (xx)
ZA (1) ZA201009075B (xx)

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20110061298A1 (en) * 2009-09-14 2011-03-17 General Electric Company Method and apparatus for drying solid feedstock using steam
US20120121477A1 (en) * 2009-07-17 2012-05-17 Green Energy And Technology Sdn Bhd Thermal gasification reactor for producing heat energy from waste
CN103084129A (zh) * 2011-10-28 2013-05-08 北京低碳清洁能源研究所 多段等离子体裂解碳质材料反应器及用其生产乙炔的方法
US20140102000A1 (en) * 2011-06-23 2014-04-17 Michael Haube Gasifier for solid carbon fuel
US8721748B1 (en) * 2013-01-28 2014-05-13 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
US20140209447A1 (en) * 2011-09-01 2014-07-31 Guradoor, S.L. Gasification-pyrolysis dual reactor device
US9278314B2 (en) 2012-04-11 2016-03-08 ADA-ES, Inc. Method and system to reclaim functional sites on a sorbent contaminated by heat stable salts
US9352270B2 (en) 2011-04-11 2016-05-31 ADA-ES, Inc. Fluidized bed and method and system for gas component capture
US20160168492A1 (en) * 2012-01-30 2016-06-16 PHG Energy, LLC Fluidized bed biogasifier and method for gasifying biosolids
US20170301938A1 (en) * 2009-06-02 2017-10-19 Thermochem Recovery International, Inc. Multi-reaction process for forming a product gas from solid carbonaceous material
WO2017206281A1 (zh) * 2016-06-01 2017-12-07 中油锐思技术开发有限责任公司 冷却气化装置、废水复合热载体发生器及复合热载体产生方法
WO2017212223A1 (en) * 2016-06-06 2017-12-14 Energy Technologies Institute Llp Equilibrium approach reactor
EA034468B1 (ru) * 2016-06-01 2020-02-11 Сиенписи Глобал Солюшнс Лтд. Установка для охлаждения и парообразования, генератор многокомпонентного теплоносителя на основе сточной воды и способ получения многокомпонентного теплоносителя
US20220025284A1 (en) * 2018-11-28 2022-01-27 Kbi Invest & Management Ag Reactor and process for gasifying and/or melting of feed materials
US11236278B2 (en) 2016-10-12 2022-02-01 WS-Wärmeprozeßtechnik GmbH Process for gasifying biomass with tar adsorption
US11242494B2 (en) 2013-01-28 2022-02-08 Aries Clean Technologies Llc System and process for continuous production of contaminate free, size specific biochar following gasification
US11279894B2 (en) 2012-01-30 2022-03-22 Aries Gasification, Llc Universal feeder for gasification reactors

Families Citing this family (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102191089A (zh) * 2011-03-29 2011-09-21 万贤法 两段式高温预热蒸汽生物质气化炉
US9650254B2 (en) * 2011-04-01 2017-05-16 Dalian University Of Technology Method for preparation of active carbon by pyrolysis of organics
AU2011370246B2 (en) 2011-06-10 2016-09-29 Bharat Petroleum Corporation Limited Process for co-gasification of two or more carbonaceous feedstocks and apparatus thereof
DE102012202143B3 (de) * 2012-02-13 2013-05-29 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Schlackebadvergasung fester Brennstoffe
NZ700523A (en) * 2012-05-18 2016-05-27 Japan Blue Energy Co Ltd Biomass gasifier device
KR101318980B1 (ko) 2012-09-19 2013-10-17 아주대학교산학협력단 합성 천연 가스 생성 장치 및 방법
ITTO20121122A1 (it) * 2012-12-21 2014-06-22 Salvatore Marasa Reattore di piro-gassificazione.
DE102013101368B4 (de) 2013-02-12 2023-04-27 Gidara Energy B.V. Wirbelschichtvergaser
US9376639B2 (en) * 2013-03-15 2016-06-28 Terrapower, Llc Method and system for performing gasification of carbonaceous feedstock
CN104017608B (zh) * 2014-05-14 2017-03-15 上海尧兴投资管理有限公司 射流床煤制合成气气化炉
JP6526499B2 (ja) * 2015-06-29 2019-06-05 株式会社神鋼環境ソリューション バーナ
CN105542869B (zh) * 2015-12-10 2018-09-21 上海尧兴投资管理有限公司 煤制合成气的气化炉
CN105713678A (zh) * 2016-03-11 2016-06-29 郭宾 多功能气化炉及联合循环能源系统
RU175131U1 (ru) * 2016-12-09 2017-11-22 Федеральное государственное бюджетное учреждение науки Объединенный институт высоких температур Российской академии наук (ОИВТ РАН) Устройство для термической конверсии биомассы
JP6899102B2 (ja) * 2017-09-29 2021-07-07 株式会社ジャパンブルーエナジー バイオマスのガス化装置
JP7088734B2 (ja) * 2018-05-10 2022-06-21 エネサイクル株式会社 改質炉
GB201900676D0 (en) * 2019-01-17 2019-03-06 Chalabi Rifat Al Process for producing activated carbon and hydrogen
JP7341075B2 (ja) * 2020-01-22 2023-09-08 三菱重工業株式会社 ガス化システム及びガス化方法
CN112029538B (zh) * 2020-08-17 2021-09-24 新奥科技发展有限公司 粉煤与块煤的耦合气化系统及方法
KR102312365B1 (ko) * 2021-03-26 2021-10-15 주식회사 한양 에프엔티 고온 개질기
KR102467994B1 (ko) * 2021-05-11 2022-11-17 주식회사 한양 에프엔티 캡슐형 개질로를 갖는 고온 개질기
WO2023102579A1 (en) * 2021-12-01 2023-06-08 Cochrane William Thomas Gasifier

Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3817723A (en) * 1972-03-23 1974-06-18 Secretary Two-stage gasification of pretreated coal
US3844733A (en) * 1972-03-23 1974-10-29 Us Interior Two-stage downflow gasification of coal
US3945809A (en) * 1975-07-08 1976-03-23 The United States Of America As Represented By The United States Energy Research And Development Administration Method and apparatus for removing coarse unentrained char particles from the second stage of a two-stage coal gasifier
US4069024A (en) * 1977-05-09 1978-01-17 Combustion Engineering, Inc. Two-stage gasification system
US4177740A (en) * 1978-03-10 1979-12-11 Enterprises International, Inc. Apparatus for generating heat from waste fuel
US4422857A (en) * 1980-08-27 1983-12-27 Firma Carl Still Gmbh & Kg Coke gasification method
US6074623A (en) * 1997-10-14 2000-06-13 Vick; Steven C. Process for thermal destruction of spent potliners
US6647903B2 (en) * 2000-09-14 2003-11-18 Charles W. Aguadas Ellis Method and apparatus for generating and utilizing combustible gas
US20030233788A1 (en) * 2001-03-12 2003-12-25 Lewis Frederick Michael Generation of an ultra-superheated steam composition and gasification therewith
US20040060236A1 (en) * 2001-01-18 2004-04-01 Kunio Yoshikawa Apparatus for gasifying solid fuel
US6837910B1 (en) * 1999-09-20 2005-01-04 Japan Science And Technology Agency Apparatus and method for gasifying liquid or solid fuel
US6960234B2 (en) * 2000-12-04 2005-11-01 Emery Energy Company, L.L.C. Multi-faceted gasifier and related methods

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2086411B (en) * 1980-10-27 1984-03-28 British Gas Corp Efg process
GB8423949D0 (en) * 1984-09-21 1984-10-31 English Electric Co Ltd Fluidised-bed gasifier
JP3572121B2 (ja) * 1995-08-21 2004-09-29 三菱重工業株式会社 有機系廃棄物のガス化炉及びガス化方法
CN100519706C (zh) * 2003-12-31 2009-07-29 财团法人工业技术研究院 一种碳化物气化反应系统
JP5107903B2 (ja) * 2005-05-02 2012-12-26 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 合成ガスの製造方法及びシステム
JP2008542481A (ja) * 2005-06-03 2008-11-27 プラスコ エネルギー グループ インコーポレーテッド 石炭を特定の組成のガスへ変換するためのシステム
GR1005536B (el) * 2006-03-07 2007-06-07 Λαμπρος Ελευσινιωτης Διβαθμιος συνδυασμενος αεριοποιητης ομορροης -αντιρροης
WO2008013794A2 (en) * 2006-07-24 2008-01-31 Clean Energy, L.L.C. Conversion of carbonaceous materials to synthetic natural gas by pyrolysis, reforming, and methanation

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3817723A (en) * 1972-03-23 1974-06-18 Secretary Two-stage gasification of pretreated coal
US3844733A (en) * 1972-03-23 1974-10-29 Us Interior Two-stage downflow gasification of coal
US3945809A (en) * 1975-07-08 1976-03-23 The United States Of America As Represented By The United States Energy Research And Development Administration Method and apparatus for removing coarse unentrained char particles from the second stage of a two-stage coal gasifier
US4069024A (en) * 1977-05-09 1978-01-17 Combustion Engineering, Inc. Two-stage gasification system
US4177740A (en) * 1978-03-10 1979-12-11 Enterprises International, Inc. Apparatus for generating heat from waste fuel
US4422857A (en) * 1980-08-27 1983-12-27 Firma Carl Still Gmbh & Kg Coke gasification method
US6074623A (en) * 1997-10-14 2000-06-13 Vick; Steven C. Process for thermal destruction of spent potliners
US6837910B1 (en) * 1999-09-20 2005-01-04 Japan Science And Technology Agency Apparatus and method for gasifying liquid or solid fuel
US6647903B2 (en) * 2000-09-14 2003-11-18 Charles W. Aguadas Ellis Method and apparatus for generating and utilizing combustible gas
US6960234B2 (en) * 2000-12-04 2005-11-01 Emery Energy Company, L.L.C. Multi-faceted gasifier and related methods
US20040060236A1 (en) * 2001-01-18 2004-04-01 Kunio Yoshikawa Apparatus for gasifying solid fuel
US20030233788A1 (en) * 2001-03-12 2003-12-25 Lewis Frederick Michael Generation of an ultra-superheated steam composition and gasification therewith

Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10854903B2 (en) * 2009-06-02 2020-12-01 Thermochem Recovery International, Inc. Multi-reaction process for forming a product gas from solid carbonaceous material
US20170301938A1 (en) * 2009-06-02 2017-10-19 Thermochem Recovery International, Inc. Multi-reaction process for forming a product gas from solid carbonaceous material
US9568189B2 (en) * 2009-07-17 2017-02-14 Green Energy And Technology Sdn Bhd Thermal gasification reactor for producing heat energy from waste
US20120121477A1 (en) * 2009-07-17 2012-05-17 Green Energy And Technology Sdn Bhd Thermal gasification reactor for producing heat energy from waste
US9085738B2 (en) * 2009-09-14 2015-07-21 General Electronic Company Method and apparatus for drying solid feedstock using steam
US20110061298A1 (en) * 2009-09-14 2011-03-17 General Electric Company Method and apparatus for drying solid feedstock using steam
US9352270B2 (en) 2011-04-11 2016-05-31 ADA-ES, Inc. Fluidized bed and method and system for gas component capture
US9228143B2 (en) * 2011-06-23 2016-01-05 Xylowatt S.A. Gasifier for solid carbon fuel
US9926500B2 (en) 2011-06-23 2018-03-27 Xylowatt S.A. Gasifier for solid carbon fuel with active transfer means
US20140102000A1 (en) * 2011-06-23 2014-04-17 Michael Haube Gasifier for solid carbon fuel
US20140209447A1 (en) * 2011-09-01 2014-07-31 Guradoor, S.L. Gasification-pyrolysis dual reactor device
CN103084129A (zh) * 2011-10-28 2013-05-08 北京低碳清洁能源研究所 多段等离子体裂解碳质材料反应器及用其生产乙炔的方法
US20160168492A1 (en) * 2012-01-30 2016-06-16 PHG Energy, LLC Fluidized bed biogasifier and method for gasifying biosolids
US11279894B2 (en) 2012-01-30 2022-03-22 Aries Gasification, Llc Universal feeder for gasification reactors
US9809769B2 (en) * 2012-01-30 2017-11-07 Aries Gasification, Llc Fluidized bed biogasifier and method for gasifying biosolids
US9278314B2 (en) 2012-04-11 2016-03-08 ADA-ES, Inc. Method and system to reclaim functional sites on a sorbent contaminated by heat stable salts
US11566191B2 (en) 2013-01-28 2023-01-31 Aries Clean Technologies Llc System and process for continuous production of contaminate free, size specific biochar following gasification
US8721748B1 (en) * 2013-01-28 2014-05-13 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
US9375694B2 (en) 2013-01-28 2016-06-28 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
US11242494B2 (en) 2013-01-28 2022-02-08 Aries Clean Technologies Llc System and process for continuous production of contaminate free, size specific biochar following gasification
WO2017206281A1 (zh) * 2016-06-01 2017-12-07 中油锐思技术开发有限责任公司 冷却气化装置、废水复合热载体发生器及复合热载体产生方法
EA034468B1 (ru) * 2016-06-01 2020-02-11 Сиенписи Глобал Солюшнс Лтд. Установка для охлаждения и парообразования, генератор многокомпонентного теплоносителя на основе сточной воды и способ получения многокомпонентного теплоносителя
WO2017212223A1 (en) * 2016-06-06 2017-12-14 Energy Technologies Institute Llp Equilibrium approach reactor
US11236278B2 (en) 2016-10-12 2022-02-01 WS-Wärmeprozeßtechnik GmbH Process for gasifying biomass with tar adsorption
US20220025284A1 (en) * 2018-11-28 2022-01-27 Kbi Invest & Management Ag Reactor and process for gasifying and/or melting of feed materials
US11788021B2 (en) * 2018-11-28 2023-10-17 Kbi Invest & Management Ag Reactor and process for gasifying and/or melting of feed materials

Also Published As

Publication number Publication date
SE0801266A0 (sv) 2009-12-21
SE1051371A1 (sv) 2010-12-22
SE534810C2 (sv) 2011-12-27
EA201001822A1 (ru) 2011-06-30
BRPI0912280A2 (pt) 2015-10-20
CN102076830A (zh) 2011-05-25
CA2726250A1 (en) 2009-12-03
AP2010005514A0 (en) 2010-12-31
EA017739B1 (ru) 2013-02-28
EP2300568A2 (en) 2011-03-30
ZA201009075B (en) 2012-09-26
JP2011522084A (ja) 2011-07-28
AU2009251931A1 (en) 2009-12-03
WO2009145724A2 (en) 2009-12-03
WO2009145724A3 (en) 2010-08-12

Similar Documents

Publication Publication Date Title
US20110078951A1 (en) Two-stage high-temperature preheated steam gasifier
EP1348011B1 (en) Multi-faceted gasifier and related methods
RU2600373C2 (ru) Частичное окисление метана и высших углеводородов в потоках синтез-газа
Skoulou et al. Low temperature gasification of olive kernels in a 5-kW fluidized bed reactor for H2-rich producer gas
US20190153341A1 (en) Process for co-gasification of two or more carbonaceous feedstocks and apparatus thereof
US8043390B2 (en) Apparatus and method for controlling the gas composition produced during the gasification of carbon containing feeds
US8668753B2 (en) Two stage process for converting biomass to syngas
KR101633951B1 (ko) 재생연료를 추가 및 후-가스화하여 합성가스의 엔탈피를 이용하기 위한 방법 및 장치
WO2007081296A1 (en) Downdraft/updraft gasifier for syngas production from solid waste
JP2012522870A (ja) ２段階乾燥供給ガス化装置および方法
CA2834052A1 (en) Gasification of bio-oil and alkali containing energy rich aqueous solutions from pulp mills
EP2752476A1 (en) Gasification-pyrolysis dual reactor device
WO2021191925A1 (en) Gasification system design and process for reduction in tar formation
CA3196638A1 (en) Process for gasifying an organic material and plant for carrying out said process
Mujiarto et al. The Effect of Temperature Controller on the Gasification Performance Using Downdraft Gasifier with Three-Stages Gasifying Agent
JP2008169354A (ja) 石炭の水素化熱分解方法及び装置
AU2002230588B2 (en) Multi-faceted gasifier and related methods
Vegman 93lQ3742 Coal gasification in molten slag to manufacture reducing gas for smelting in blast furnaces
AU2002230588A1 (en) Multi-faceted gasifier and related methods

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION