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WO2018065466A1 - Commande de flux de réacteur - Google Patents

Commande de flux de réacteur Download PDF

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Publication number
WO2018065466A1
WO2018065466A1 PCT/EP2017/075222 EP2017075222W WO2018065466A1 WO 2018065466 A1 WO2018065466 A1 WO 2018065466A1 EP 2017075222 W EP2017075222 W EP 2017075222W WO 2018065466 A1 WO2018065466 A1 WO 2018065466A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
gasification chamber
char
oxidant
gas
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.)
Ceased
Application number
PCT/EP2017/075222
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English (en)
Other versions
WO2018065466A9 (fr
Inventor
Anders Wingren
Niklas STRANDBERG
Niclas Davidsson
Rikard Öhman
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.)
MEVA ENERGY AB
Original Assignee
MEVA ENERGY AB
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 MEVA ENERGY AB filed Critical MEVA ENERGY AB
Publication of WO2018065466A1 publication Critical patent/WO2018065466A1/fr
Publication of WO2018065466A9 publication Critical patent/WO2018065466A9/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • 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
    • C10J3/22—Arrangements or dispositions of valves or flues
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • C10J2300/0953—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
    • C10J2300/0959—Oxygen

Definitions

  • the present invention generally relates to conversion of carbonaceous materials into desirable gaseous products such as synthesis gas. More specifically the present invention relates to a gasification system for gasifying carbonaceous material and a method thereof.
  • Gasification can be described as a process where organic or fossil fuel based carbonaceous materials are converted into a product gas of varying molecular weights, such as e.g. carbon monoxide, hydrogen and carbon dioxide. This is generally achieved through a thermo-chemical reaction where the carbonaceous materials react with a controlled amount of oxygen, steam and/or carbon dioxide acting as an oxidant, the resulting product gas mixture is often called synthesis gas (also known as synthetic gas or syngas).
  • synthesis gas also known as synthetic gas or syngas
  • the synthesis gas can later be used as a fuel gas where it is burned directly as fuel to produce heat and/or electric power or as an intermediate for other multiple uses.
  • the power derived from gasification of bio-based feedstock is considered to be a source of renewable energy and the gasification industry has attracted a lot of interest during these last decades.
  • gasification differs from other, more traditional energy- generating processes, in that it is not a combustion process, but rather a conversion process.
  • the feedstock to be gasified is incompletely combusted to create the syngas which then at a later stage is completely combusted in order to release the remaining energy.
  • the atmosphere within the chamber is deprived of oxygen, and the result is complex series of reactions of the feedstock to produce synthesis gas.
  • the synthesis gas can be cleaned relatively easily, given the much lower volume of raw synthesis gas to be treated compared to the large volume of flue gases that need to be treated in conventional post-combustion cleaning processes.
  • a gasification system for gasifying a carbonaceous material wherein the gasification system comprises:
  • a gasification chamber having an upper section and a lower section; at least one screw-feeder for injecting and dispersing a carbonaceous solid fuel with a particle size of less than 10 mm (and oxidant in some embodiments) into the upper section whereby synthesis gas and residual char is generated by a first thermo-chemical reaction occurring during a downwardly directed falling of the carbonaceous fuel towards a bottom portion of the lower section;
  • a char bed disposed in the lower section, the char bed being formed by residual char generated in the first thermo-chemical reaction;
  • At least one gas-inlet at a bottom portion of the lower section for injecting oxidant into the char bed whereby synthesis gas is generated by a second thermo-chemical reaction from the residual char;
  • the at least one screw feeder is arranged at a predefined distance from the bottom portion, wherein the predefined distance is at least 30% of a vertical extension of the gasification chamber, preferably the predefined distance is at least 50 % of the vertical extension of the
  • the gasification chamber and most preferably the predefined distance is 60% of the vertical extension of the gasification chamber.
  • the gasification system according to the first aspect of the present invention is less complex and more cost-effective as compared to known prior art solutions and efficiently utilizes the residual char from the first thermo-chemical reaction to form a char bed.
  • the gasification system further has a gas-inlet at the bottom portion of the lower section for injecting oxidant into the char bed in order to form an at least partly fluidizing/fluidized char bed whereby a second thermo-chemical reaction can occur in order to increase the synthesis gas output of the system.
  • the oxidant can for example be air, steam or oxygen while the carbonaceous particulate fuel can for example be one or more of the following: biomass, biofuel, coal, wood, agricultural residues such as e.g. husk, digestate, manure, dewatered waste water, barch, straw, peat, fibre residue.
  • the gasification system may be provided with one or more oxidant inlets at the upper section which is/are independent from the screw-feeder and/or oxidant may be injected via the same screw-feeder as the carbonaceous solid fuel.
  • the gasification chamber is preferably cylindrically shaped and has a cylindrical inner wall/surface enclosing an internal cavity.
  • the inner wall of the gasification chamber can be at least partly curved, e.g. by being cylindrically shaped such that a part of said curved wall forms part of a cylinder.
  • a cross section of said gasification chamber is circular, the cross section being in a plane
  • the lower section may have an inner wall/surface with a tapered cylindrical (i.e. conical) character where a bottom portion has the smallest diameter, however, configurations where the gasification chamber has a more uniform character are also feasible, i.e. the upper section and the lower section may be arranged to have the same diameter.
  • the upper section and the lower section of the gasification chamber are preferably portions of a single vessel or container or at least in fluid connection with each other.
  • the present invention is based on the realization that conversion of carbonaceous matter to synthesis gas (or syngas) occurs step-wise by means of different thermo-chemical reactions with differing reaction conditions and that such differing reactions can be created in a single chamber gasification reactor.
  • the invention is based on the realization that the first release of volatiles (volatile matter) occurs more rapidly and at a lower temperature than the following gasification of carbon which demands a longer residence time and higher temperature.
  • the present inventors realized that by arranging controlled falling of fine fraction carbonaceous fuel from a top section to a lower section of a gasification chamber, a first thermo-chemical reaction (flash pyrolysis) of said fuel can be achieved.
  • the gravitational falling also provides an advantageous condition as it means that the fuel is dispersed in the hot gas of the gasification.
  • a high level of such dispersion is achieved by the injecting of the feedstock into the gasification chamber due to the usage of a screwfeeder as feeding device.
  • Such dispersion increases the contact area between the fuel and the gas which enhances the thermo-chemical reactivity.
  • Other injection means such as for example pneumatically by the using a blower means that the feedstock enters with a higher velocity thereby inhibiting the spread (dispersion) of the feedstock in the surrounding gas.
  • Blower-fed injectors tend to push the feedstock towards the inner wall of the gasification chamber thereby inhibiting the desired maximized mixing of the feedstock with the gas.
  • screw-feeding in contrast to blowing, enables that only a small amount of oxidizing air is injected in the same injector as the feedstock. In this way the distribution of oxidant in the gasification chamber can be controlled as more oxidant can be injected at other locations in the gasification chamber than directly with the feedstock injection.
  • the residence time of the carbonaceous fuel during the downwardly directed falling is preferably at least 1 second and more preferably at least 2 seconds, in order to for example ensure release of volatile matter in the first thermo-chemical reaction.
  • the residence time of the carbonaceous fuel during the downwardly directed falling can for example be controlled by controlling the position of the screw feeder at the gasification chamber, injection velocities of fuel or oxidant, oxidant supply, etc.
  • the residence time of the first thermo-chemical reaction can be controlled by determining the distance between the fuel injector and the bottom portion of the gasification reactor and by the injection velocities of feedstock and oxidant.
  • the complete gasification system enables increased energy efficiency as compared to prior known solutions.
  • unnecessary heating of the volatile gas generated by the flash pyrolysis (first thermo-chemical reaction) is avoided, thereby minimizing the combustion of such volatile gas. This would be the case if the residual char was converted to synthesis gas in the same section as the first thermo-chemical pyrolysis process (upper section in the present context).
  • the pyrolysis process can be said to be a process where volatile matter in the carbonaceous particulate material are released and converted to permanent gases, pyrolysis-oil and tar. Furthermore, the residual char is efficiently handled and utilized (for forming the hot fluidizing bed) whereby costs can be reduced since there is no need to lead off the extremely high temperature residual char particles, e.g. via the same outlet as the syngas is extracted, as in more conventional systems.
  • the gasification system further has at least one outlet for extracting the produced syngas, the at least one outlet may for example be arranged at a top portion of the gasification chamber. The top portion is to be understood in the context of the present application as a top-most portion of the upper section. Stated differently, the gasification system may further comprise a syngas exit pipe arranged at a top portion of the gasification chamber, where the syngas exit pipe has an opening arranged the gasification chamber for receiving the synthesis gas.
  • the gasification chamber according to the first aspect of the present invention has two different sections, namely the upper section and the lower section. These two sections may, to some extent, be referred to as a "cold” section and a “hot” section, respectively, where volatile matters in the carbonaceous fuel are gasified in a flash pyrolysis reaction in the upper section (cold), and char is gasified in a carbon
  • the gasification system is configured to maintain the residual char within the gasification chamber after the first thermo-chemical reaction in order to form a char bed at the lower section with the residual char.
  • the residual char is kept from exiting the same outlet as the generated/produced synthesis gas by controlling the injection parameters of the injected fuel and/or the oxidant at the bottom gas-inlet. This diminishes the need for handling the often extremely hot residual char in any piping connected to the one or more outlets which reduces the cost of the gasification system.
  • the present invention relies on gasification with very limited combustion of the carbonaceous particulate fuel, as opposed to many known prior solutions, where complete combustion is included in at least one process step.
  • the cold gas efficiency can be increased.
  • the particulate fuel comprises particles with a particle size of less than 3 mm and a moisture ratio of not more than 30 wt%.
  • 80 % or more of the particulate fuel comprises particles with a particle size of less than 3 mm and a moisture ratio of not more than 30 wt%.
  • additional substance besides oxidant and particulate fuel such as e.g. catalysts or inert substance or e.g. sand or carbon dioxide, are injected into the upper section via the at least one fuel inlet or a secondary inlet.
  • the oxidant injection through said at least one gas-inlet is arranged such that an injection velocity of said injected oxidant into said char bed is controlled such that a fluidization of said char bed does not disrupt a balance between the downwardly directed falling of residual char from said upper section and upwardly directed flow of gas (within the gasification chamber).
  • the injection velocity of the oxidant injection at the bottom portion such that the upwardly directed gas velocity in the gasification chamber is kept within e.g. an interval of 0.1 to 2.0 m/s, the risk of disrupting/destroying the (fluidized) char bed, and consequently being forced to handle the residual char together with the generated and extracted synthesis gas, is reduced.
  • This also enables the injection of light weight carbonaceous particulate fuel, while still being able to form a
  • gas velocity is in reference to the gas traveling within the chamber, and not to the injection velocity of the oxidant, as the injection velocity is most often higher and depends on various structural details such as e.g. size and shape of the gas inlet(s) which can be varied depending on desired specifications or applications.
  • the gas velocity is at least partly set or limited based on the
  • the gas injection velocity is controlled in order to keep the upwardly and downwardly directed flows in balance such that the bed material (residual char) of the fluidizing char bed isn't scattered upwards within the chamber.
  • the residual char generated from the thermo-chemical gasification/pyrolysis process in the upper section of the gasification chamber, is allowed to travel downwards toward the lower section and to form the (fluidized) char bed.
  • the oxidant injection through said at least one gas-inlet is arranged such that a supply of oxidant into the char bed is in the range of 40-80% of a total oxidant supply into the gasification chamber.
  • the screw-feeder may, in some embodiments, be configured to inject carbonaceous fuel with an injection velocity being less than 5 m/s.
  • the upper section of the gasification chamber has a curved inner surface, and wherein the solid particulate carbonaceous fuel and the oxidant are (concurrently) injected into the upper section and dispersed in the gasification chamber such that a entrained flow of the synthesis gas is formed and whereby residual char is separated and allowed to travel from the upper section down towards the lower section in order to form the char bed.
  • the gasification reactions occurs in a dense cloud of fuel particles that is fed into the gasification chamber where it forms a plume falling down towards the bottom portion of the lower section of the chamber.
  • a plume may in the present context be understood as an elongated cloud of gas or vapour resembling a feather as it spreads from its point of origin.
  • These types of gasification chambers are often referred to as entrained flow reactors or entrained flow gasifiers.
  • the term "entrained flow” is in reference to a concurrent injection (or feeding) of the carbonaceous fuel particles and the oxidant, where the oxidant flow can for example act as a carry for the fuel particles.
  • an entrained flow gasifier is specifically suitable for use with pulverized fuel, whereby oxidant being injected together with the fuel is consumed in the first thermo-chemical reaction.
  • the screw-feeder is protruding into the gasification chamber so that the fuel is evenly distributed as a plume in the gasification chamber.
  • the screw-feeder is arranged to protrude into the gasification chamber in order to more evenly spread the (particulate) carbonaceous fuel and utilize the volume of the gasification chamber in a more efficient manner. This further increases the contact area between the carbonaceous fuel particles and the gas which enhances the thermo-chemical reactivity.
  • the screw-feeder may for example be arranged to protrude into the gasification chamber by at least 30% of the distance from a sidewall to a central vertical axis, in other words, by at least 30% of the radius of the gasification chamber (if approximated as a cylinder).
  • the gasification chamber further comprises one or more temperature control inlets arranged through a side-wall of said gasification chamber.
  • the temperature control inlet(s) is/are configured to inject oxidant into the gasification chamber whereby a process temperature within said gasification chamber is controlled.
  • the injected gas can for example be air, steam or oxygen.
  • the one or more temperature inlets can be spatially separated and distributed along a (vertical) length of the gasification chamber, i.e. being serially arranged in a side-wall of the gasification chamber from a top to a bottom of the gasification chamber.
  • the gasification chamber may comprise a temperature control inlet arranged at the upper section, a temperature control inlet at the lower section and a temperature control inlet at a mid section (between the upper section and the lower section).
  • the temperature control inlets are preferably individually controllable in terms of injection rates for the injected gas.
  • the temperature control inlets may for example be configured to maintain a temperature at the upper section of the gasification chamber in the range of 800°C to 1 100°C, and to maintain a temperature of the (at least partly fluidized) char bed at the lower section in the range of 1200°C to 1500°C, in order to ensure that the first thermo-chemical reaction is a flash pyrolysis reaction and the second thermo-chemical reaction is a carbon gasification reaction.
  • the fuel is pre-heated by a preheating arrangement whereby the needed residence time of the particulate carbonaceous fuel within the gasification chamber can be reduced.
  • preheating may be accomplished by using the fuel inlet, to inject a fuel together with an oxidant in order to provide for an exothermic reaction between the fuel and the oxidant. This exothermic reaction will thus pre-heat the fuel before the injecting into the gasification chamber.
  • An optional alternative for pre-heating is to pre-heat the particulate carbonaceous fuel and the oxidant in the screw-feeder, i.e. before it is injected into the upper section via the fuel-inlet.
  • the gasification system further comprises a perforated grate located at said bottom portion, in order to facilitate extraction of residual ashes.
  • a method for gasifying carbonaceous material comprising: providing a gasification chamber having an upper section, a lower section and a screw-feeder arranged at a predefined distance from the bottom portion, the predefined distance being at least 30% of a vertical extension of the gasification chamber;
  • a carbonaceous solid fuel being less than 10 mm in diameter (and oxidant in some embodiments) into the upper section of the gasification chamber whereby synthesis gas and residual char is generated in a first thermo-chemical reaction occurring during a downwardly directed falling of the carbonaceous fuel towards a bottom portion of the lower section ;
  • the method may further comprise a step of extracting the synthesis gas from a top portion of said gasification chamber.
  • the injection parameters of the oxidant via the one or more gas inlets may for example be injection velocity and/or an injection amount/supply in reference to the total oxidant supply into the gasification chamber.
  • the supply of oxidant via the at least one gas inlet into the char bed may be in the range of 40 - 80 % of a total oxidant supply into the gasification chamber or the injection velocity may be controlled such that an upwardly directed gas velocity within the gasification chamber is in the range of 0.1 - 2.0 m/s.
  • the method further comprises:
  • the gasification chamber will have two zones or section with different temperatures, whereby an efficient gasification method with increased energy output can be achieved.
  • the temperature in the upper section may for example over 900°C, and the temperature in the lower section and more specifically in the char bed may be over 1300°C.
  • the gasification system can be configured such that the first thermo-chemical reaction is a flash pyrolysis reaction and the second thermo-chemical reaction is a carbon gasification reaction.
  • Fig. 1 is a schematic illustration of a gasification system in accordance with an embodiment of the present invention
  • Fig. 2 illustrates a cross-sectional view of a gasification system in accordance with an embodiment of the invention
  • Fig. 3 is a schematic flow chart illustration a method for gasifying carbonaceous material in accordance with an embodiment of the present invention.
  • Fig. 1 a schematic illustration of a gasification system 1 is provided.
  • the gasification system includes a gasification chamber 2, shown in a cross- sectional view where the cross-section is taken in a vertical plane including a longitudinal vertical axis 101 .
  • the gasification chamber 2 has an inner and an outer wall, and the chamber may for example be made of a ceramic material.
  • the gasification chamber 2 has an upper section 3 and a lower section 4 and a screw-feeder or screw-feeding device 8.
  • the screw feeding device is arranged to inject and disperse a carbonaceous solid fuel with a particle size of less than 10 mm into the upper section 3 whereby synthesis gas and residual char is generated by a first thermo-chemical reaction occurring during a downwardly directed falling of the particulate carbonaceous fuel towards a bottom portion of said lower section 3.
  • the first thermo-chemical reaction is preferably a flash pyrolysis reaction.
  • the injection velocity of the carbonaceous fuel is preferably less than 5 m/s.
  • the screw-feeder 8 may also be configured to inject oxidant into the gasification chamber 2, however, oxidant may be injected into the gasification chamber via one or more separate oxidant inlets.
  • the screw-feeder 8 can include a preheating arrangement (not shown) in order to preheat the carbonaceous fuel before it is injected into the gasification chamber 2.
  • the preheating arrangement can for example include a fluid channel extending through the screw-feeder 8, and where a hot gas is allowed to flow through the fluid channel so that the particulate carbonaceous fuel is preheated while it is travels helically through the screw-feeder 8.
  • the gasification system 1 has a char bed 12 disposed in the lower section 4.
  • the char bed 12 is formed by residual char generated in the first thermo-chemical reaction, which travels downwards due to gravitational force towards the bottom portion 5.
  • the bottom portion 5 can for example be said to be defined by a bottom surface upon which the residual char generated by the first thermo-chemical reaction is collected.
  • the lower section comprises a supporting surface (for example in the form of a perforated grate 15) arranged to support a formation of a char bed on top of said supporting surface.
  • thermo-chemical reaction there is at least one gas inlet 17 at the bottom portion 5 through which oxidant can be injected into the formed char bed 12 in order to create a second thermo-chemical reaction whereby synthesis gas is generated from the residual char.
  • the second thermo- chemical reaction is preferably a carbon gasification reaction.
  • synthesis gas is generated by two different thermo-chemical reactions at different sections of the gasification chamber 2, which increases the overall output of synthesis gas and thereby the efficiency of the gasification system 1 .
  • the two sections 3, 4 are preferably part of one single vessel or container and consequently the two thermo-chemical reactions occur within the same vessel or container.
  • the bottom portion 5 further includes a supporting surface in the form of a perforated grate 15 on top which supports the char bed 12, and which is used to extract residual ashes.
  • the gasification chamber 2 comprises an outlet at the bottom portion through which residual ash particles may exit the gasification chamber.
  • the outlet is at least partly blocked by the perforated grate 15 in order to support the formation of the char bed 12, however, the perforated grate 15 (i.e. the supporting surface) may for example be movable (by an operator or an actuator) in order to extract any residual ash particles collected at the bottom of the char bed 12.
  • the screw-feeder is arranged at a predefined distance 23 from the bottom portion 5, the predefined distance 23 being at least 30% of a vertical extension of the gasification chamber.
  • the dispersed carbonaceous particles have a long enough residence time in order to travel through different reaction zones within the gasification chamber 2, whereby a complete conversion of the carbonaceous fuel to synthesis gas can be achieved.
  • the gasification system allows for controlled falling of fine fraction carbonaceous fuel from the upper section 3 to the lower section 4 of the gasification chamber 2, so that a first thermo-chemical reaction (flash pyrolysis) of the fuel can be achieved.
  • the gravitational falling also provides an advantageous condition as it means that the fuel is dispersed in the hot gas of the gasification.
  • the residence time of the carbonaceous fuel during the downwardly directed falling is preferably at least one second and more preferably at least two seconds.
  • one or more injection parameters of the oxidant injection into the char bed 12 can be controlled so that a fluidization of the char bed 12 does not disrupt a balance between the downwardly directed falling of residual char from the upper section and upwardly directed flow of the injected oxidant.
  • this can be construed as the injection of oxidant is controlled so that it does negatively affect the falling residual char (and possibly even the particulate carbonaceous fuel) and consequently inhibiting the desired "falling" through the different reaction zones.
  • the injection parameters may for example be injection velocity, injection angle or the amount of injected oxidant in reference to the total oxidant supply into the gasification chamber.
  • the oxidant injection through the at least one gas-inlet 17 is arranged such that an upward gas velocity in the gasification chamber is in the range of 0.1 m/s to 2.0 m/s.
  • the gasification chamber 2 may be arranged with a set of temperature control inlets 24.
  • the temperature control inlets/oxidant inlets 24 are preferably spatially separated and distributed along a length (elongated axis 101 ) of the gasification chamber 2.
  • a set in the present context can be one or more.
  • the temperature control inlets 24 are configured to inject gas (such as e.g. air, steam or oxygen.) into the gasification chamber in order to control the temperature within the gasification chamber 2 at various sections.
  • gas such as e.g. air, steam or oxygen.
  • the oxidant injection into the gasification chamber 2 is preferably arranged such that a predefined temperature in the range of 800°C to 1 100°C is maintained at the upper section 3, and a predefined temperature in the range of 1200°C to 1500°C is maintained at the lower section 4. This will aid to ensure an optimized path through different reaction zones for the carbonaceous fuel.
  • the oxidant injection through the one or more gas-inlets 17 may be arranged so that a supply of oxidant into the char bed is in the range of 40- 80% of a total oxidant supply into the gasification chamber.
  • the ratio of oxidant injected via the one or more gas-inlets 17 at the bottom portion in refrence to the total oxidant injection is kept at 40-80% in order to ensure favourable conditions in terms of process temperatures different sections of the gasification chamber 2, fluidization of the char bed 12, residence time for the downwardly falling carbonacous fuel, etc.
  • Fig. 2 illustrates a cross-sectional top-view view of the gasification chamber 2 from Fig. 1 , taken along line A-A'.
  • the illustration shows an arrangement where the screw feeder 8 is protruding into the gasification chamber by a predefined distance P.
  • the predefined distance P is preferably at least 30% of the radius d of the gasification chamber.
  • the tip of the screw-feeder extends towards a central vertical axis (101 in Fig. 1 ) of the gasification chamber.
  • Fig. 3 illustrates a schematic flow chart describing a method 300 for gasifying carbonaceous material in accordance with an embodiment of the present invention.
  • the method 300 comprises a step of providing 301 a gasification chamber having an upper section, a lower section and a screw- feeder arranged at a predefined distance (23 in Fig. 1 ) from the bottom portion.
  • the predefined distance is at least 30% of a vertical extension of the gasification chamber.
  • a carbonaceous solid fuel being less than 10 mm in diameter is injected 302 by means of the screw-feeder, into said upper section of the gasification chamber.
  • synthesis gas and residual char is generated in a first thermo-chemical reaction occurring during a downwardly directed falling of the carbonaceous fuel towards a bottom portion of the lower section.
  • the step of injecting 302 the carbonaceous solid fuel may in some
  • embodiments also include injecting oxidant into the gasification chamber (separately or concurrently).
  • the method 300 includes a step of forming 303 a char bed in the bottom portion of said lower section from the residual char being generated in said first thermo-chemical reaction.
  • oxidant is injected 304 into the char bed via the one or more gas inlets at the bottom portion.
  • This enables enable a second thermo- chemical reaction whereby said residual char is converted to synthesis gas.
  • at least one injection parameter is controlled such that a residence time of the downward falling carbonaceous solid fuel is at least 1 second, more preferably at least 2 seconds.
  • the injection parameters may for example be injection velocity, injection angle, amount of injected oxidant in reference to the total oxidant supply into the gasification chamber, etc.
  • the method may further comprise maintaining a temperature within the gasification chamber at the upper section in the range of 800°C - 1 100°C, preferably in the range of 850°C - 1000°C and more preferably in the range of 900°C - 950°C.
  • the method can also comprise a step of maintaining a temperature of the char bed at the lower section of the gasification chamber in the range of 1200°C - 1500°C preferably in the range of 1250°C - 1400°C and more preferably in the range of 1300°C - 1350°C.
  • the temperature within the different sections or portions of the gasification chamber can for example be maintained (or controlled) by injection of oxidant into the gasification chamber via a set of temperature control inlets and/or the one or more gas inlets at the bottom portion.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

L'invention concerne également un système de gazéification et un procédé de gazéification d'un combustible carboné particulaire. Le système de gazéification comprend une chambre de gazéification ayant une section supérieure et une section inférieure avec une entrée de combustible pour injecter un combustible carboné particulaire et un oxydant dans la section supérieure, dans une réaction thermochimique, par laquelle, un gaz de synthèse et un résidu de carbonisation résiduel sont générés. Le système de gazéification comprend en outre un séparateur conçu pour recevoir le gaz de synthèse et pour séparer le goudron résiduel du gaz de synthèse. En outre, il y a un lit de produit de carbonisation disposé dans la section inférieure formée par un résidu de carbonisation résiduel généré dans la réaction thermochimique et une entrée de gaz au niveau d'une partie inférieure de la section inférieure pour injecter du gaz dans le lit de produit de carbonisation. Le goudron résiduel est injecté dans le lit de produit de carbonisation, moyennant quoi, dans un processus de craquage thermique, le goudron résiduel est converti en gaz de synthèse. Ainsi, il est possible de récupérer l'énergie perdue contenue dans le goudron résiduel, et d'obtenir ainsi un meilleur rendement dans un système de gazéification, d'une manière économique et simple.
PCT/EP2017/075222 2016-10-07 2017-10-04 Commande de flux de réacteur Ceased WO2018065466A1 (fr)

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EP16192924.5 2016-10-07
EP16192924.5A EP3305875B1 (fr) 2016-10-07 2016-10-07 Commande de flux de réacteur

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CN111826201A (zh) * 2020-06-10 2020-10-27 山东大学 一种生物质闪速热解气化并脱除焦油的工艺、系统及应用

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020020112A1 (en) * 2000-07-25 2002-02-21 Scotlund Stivers Process and apparatus for manufacturing fuel gas and liquid fuels from trash, other waste materials and solid fuels
DE202009002781U1 (de) * 2009-02-27 2009-06-10 Kbi International Ltd. Reaktor zur thermischen Behandlung eines Einsatzstoffs
US20100037519A1 (en) * 2007-07-05 2010-02-18 The Board Of Regents For Oklahoma State University Downdraft gasifier with internal cyclonic combustion chamber
CN105602623A (zh) * 2015-12-16 2016-05-25 上海理工大学 双级下吸式生物质气化炉

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020020112A1 (en) * 2000-07-25 2002-02-21 Scotlund Stivers Process and apparatus for manufacturing fuel gas and liquid fuels from trash, other waste materials and solid fuels
US20100037519A1 (en) * 2007-07-05 2010-02-18 The Board Of Regents For Oklahoma State University Downdraft gasifier with internal cyclonic combustion chamber
DE202009002781U1 (de) * 2009-02-27 2009-06-10 Kbi International Ltd. Reaktor zur thermischen Behandlung eines Einsatzstoffs
CN105602623A (zh) * 2015-12-16 2016-05-25 上海理工大学 双级下吸式生物质气化炉

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