US20090077887A1 - Method and apparatus for treating a syngas - Google Patents

Method and apparatus for treating a syngas Download PDF

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Publication number
US20090077887A1
US20090077887A1 US11/870,040 US87004007A US2009077887A1 US 20090077887 A1 US20090077887 A1 US 20090077887A1 US 87004007 A US87004007 A US 87004007A US 2009077887 A1 US2009077887 A1 US 2009077887A1
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syngas
reactor
plasma jet
gas
torch
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Ulysse Michon
Leandre Bellat
Erika Edme
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EUROPLASMA
Europlasma SA
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Europlasma SA
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Publication of US20090077887A1 publication Critical patent/US20090077887A1/en
Priority to US13/369,018 priority Critical patent/US8974555B2/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
    • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/06—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by mixing with gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/048—Composition of the impurity the impurity being an organic compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being 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
    • C10J2300/09—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
    • C10J2300/0946—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
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
    • 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
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
    • 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
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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 disclosed embodiments relate to a method and to apparatus for treating a synthesis gas or “syngas”. It also relates to a system for treating waste or biomass, which system is equipped with such treatment apparatus.
  • Autothermal gasification is, for example, a well known method whose main mechanism seeks, in oxygen under-stoichiometry and by injecting steam, to decompose carbon chains such as those contained in biomass, forest residues, household and hospital waste, soiled wood, and any other waste having high organic potential, with a view to a obtaining a syngas that is combustible and suitable for use in recycling.
  • the definite advantage procured by gasification is that, in the absence of full combustion, the organic fraction decomposes in the form of a combustible gas (fuel gas) whose “lower combustion value” or “net calorific value” (NCV) increases with decreasing presence of carbon dioxide, of water vapor, and of nitrogen, these molecules being inefficient when used in recycling as means to generate electricity, as biofuel, or in organic chemistry.
  • fuel gas whose “lower combustion value” or “net calorific value” (NCV) increases with decreasing presence of carbon dioxide, of water vapor, and of nitrogen, these molecules being inefficient when used in recycling as means to generate electricity, as biofuel, or in organic chemistry.
  • Autothermal gasification suffers from intrinsic temperature limitation which, de facto, limits the NCV of the syngas produced.
  • Treatment capacity is also limited by the variability of the incoming matter in terms of composition and grain-size, and by its humidity level and its mineral content, and in particular its heavy metal content.
  • the approach consists in extracting them from the syngas and in recycling them back into the reactor as a thermal energy source. That action, which consists in removing that carbon potential initially available in the organic material to be treated from the gasification method gives rise to a limitation of the carbon efficiency, the direct consequence of which is a limitation in the NCV.
  • Another gasification method is known, namely direct gasification using plasma. That method consists in attacking the organic material directly with plasma so as to convert it into a high-purity, high-temperature syngas.
  • the general configuration of such a method is usually as follows: one or more plasma tools deliver one or more plasma flows into a furnace fed with materials to be gasified and/or to be vitrified.
  • the furnace then hosts thermochemical reactions for transforming the materials fed in, under the direct action and/or the indirect action of the plasma flow.
  • the liquid and gas phases that result from the synthesis or from the plasma treatment are then recovered for any subsequent treatment implementing existing techniques.
  • the essential components of such installations comprise apparatus for injecting solid matter in powder form, or for injecting liquid, or indeed for injecting semi-liquid substances (sewage plant sludge, petroleum sludge).
  • the mixture of the plasma and of the materials to be gasified and/or to be vitrified does not include all of the materials, the thermochemical treatment mainly concerning an indirect process (thermal radiation coming form the refractory walls of the furnace that are heated to high temperatures under the action of the plasma). Therefore the energy transfer between the plasma and the materials is not optimized.
  • manufacturing the furnace requires the use of refractory materials whose erosion is very sensitive to the variations in temperature generated by varying energy needs corresponding to the variable chemical composition of the incoming materials, and by the periodic removal of the plasma tool for the purpose of changing electrodes.
  • the chemical natures of the gases resulting from the plasma treatment can also limit the life of the refractory linings, in particular when said gases contain chlorine.
  • An object of the disclosed embodiments is thus to propose an indirect gasification stage for indirectly gasifying organic materials using plasma with a view to transforming a gas of medium temperature, seeded with solid particles such as particles of tar and/or of solid carbon, coming from an autothermal pyrolysis or gasification reactor in order to obtain a syngas having high purity, and having reinforced carbon potential, and whose main components are carbon monoxide and hydrogen (dihydrogen).
  • the disclosed embodiments provide a method of treating a synthesis gas or “syngas”.
  • this method comprises the following steps:
  • propagation axis that is substantially collinear with the main axis of the torch is used to mean that the propagation axis of the plasma jet is either collinear with or coincides with the axis of the torch, or else that the volume of space occupied on average over time by the plasma jet has its axis coinciding with the main axis of the plasma torch.
  • the end of the plasma jet can be placed on either side of the main axis of the torch.
  • the plasma jet occupies on average over time a position that coincides with the main axis of the torch.
  • longitudinal axis of the reactor that is substantially collinear with the propagation axis is used to mean that the longitudinal axis is either collinear with or coincides with the propagation axis, or else that said longitudinal axis is substantially aligned on said propagation axis.
  • placed downstream from is used to mean placed beyond, in the propagation direction of the plasma jet.
  • the method of treatment of the disclosed embodiments offers the advantage of being highly flexible and of adapting to accommodate all of the situations encountered in implementing a gasification method, with a single aim: to reinforce the working potential of the carbon contained in the syngas to be treated, and to make the composition of said syngas tend towards two majority elements only, namely carbon monoxide (CO) and dihydrogen (H 2 ).
  • CO carbon monoxide
  • H 2 dihydrogen
  • the plasma jet With its 5000° K on average is a flow of ionized gaseous matter, in extinction, electrically neutral, and seeded with species such as electrons, ions, atoms, and radicals having high chemical reactivity.
  • the radicals preferably go to re-associate with the species released by cracking of the non-advantageous molecules of the syngas to be treated brought up to temperature.
  • the triatomic molecules (CO 2 , H 2 O) and the molecules having even more atoms (CH 4 , C n H m ) that have low atomic bonding potential break apart and tend to produce carbon monoxide (CO) and additional dihydrogen (H 2 ).
  • the syngas is fed in in a direction that is distinct from the propagation axis so as to establish a turbulent mixing zone between the plasma jet and the syngas;
  • At least one fluid is fed into the feed enclosure and/or into the reactor in order to adjust the composition of the syngas to be treated;
  • said at least one fluid can be fed in by at least one injector, at least one injection orifice for injecting a protective fluid, the plasma torch, or a combination of said elements;
  • this fluid may be chosen from the group comprising water, carbon dioxide, and a combination of these elements;
  • the speed of the syngas/plasma jet mixture is reduced at the inside wall of the feed enclosure and/or of the reactor;
  • the reduction in the speed of the mixture can be obtained by feeding in a protective fluid tangentially to the wall of the feed enclosure and/or of the reactor, said fluid being at ambient temperature; this fluid also makes it possible to protect the refractory materials with which the feed enclosure and the reactor are advantageously equipped;
  • this reduction in speed can also be obtained by increasing the through cross-section of the plasma jet with the presence of a flared portion in the feed enclosure in order to optimize injection of said at least one fluid for adjusting the composition of the syngas to be treated;
  • the outlet gas is accelerated in the downstream portion of the reactor prior to it being extracted via the outlet port;
  • the outlet gas is quenched so as to set said outlet gas
  • the component species of the outlet gas are thus set, thereby preventing any recombination of said species, which would give rise to a reduction in the majority species H 2 and CO;
  • a protective fluid at ambient temperature is fed in tangentially to the walls of the feed enclosure and/or of the reactor, over at least a portion of said walls;
  • this protective fluid makes it possible to protect the walls of the feed enclosure and/or of the reactor from the plasma jet;
  • the temperature of the outlet gas is measured and the temperature of the plasma jet is adjusted so as to control the conversion of said syngas into outlet gas.
  • the disclosed embodiments also provide apparatus for implementing the method as described above. According to the disclosed embodiments, said apparatus comprises:
  • a feed enclosure to which a reactor is connected, the feed enclosure and the reactor each having an internal volume defined by walls covered at least partially with refractory elements, said enclosure and said reactor being in fluid communication;
  • the feed enclosure includes a non-transferred-arc plasma torch having a main axis, said torch serving to generate a plasma jet having a propagation axis that is substantially collinear with the main axis of said torch;
  • the feed enclosure is provided with at least one inlet port ( 7 ) placed downstream from the plasma torch ( 3 ) for the purpose of feeding in a syngas in a manner such that said syngas is mixed with the plasma jet; and
  • the reactor has a substantially cylindrical elongate shape, the longitudinal axis of said reactor being substantially collinear with the propagation axis of the plasma jet, said reactor having an outlet port for the outlet gas in its downstream portion.
  • This system can be said to have an “in-line” configuration, i.e. the plasma torch, then the injection apparatus, then the reactor, as opposed to the conventional configuration in which the reactor is coupled simultaneously (in “parallel”) to the torch and to the injection apparatus for injecting the material to be treated.
  • This in-line configuration offers numerous advantages, in particular it is very simple to operate, it has a suction effect whereby the syngas is sucked in by the plasma jet, and it also offers entrainment of the syngas/plasma jet mixture along a straight line (propagation axis) thereby minimizing any interactions between the overheated mixture and the walls of the feed enclosure and of the reactor.
  • the intimate mixture of the syngas and of the plasma jet also makes it possible to transfer energy directly between the plasma jet and the syngas, thereby making it possible not only to consume less energy but also to achieve syngas/plasma jet mixture temperatures that are higher than with prior art apparatus.
  • the apparatus further comprises a fluid injector for adjusting the composition of said syngas to be treated, said at least one injector serving to feed said fluid in substantially in the direction in which the syngas/plasma jet mixture flows;
  • said downstream portion includes a flared segment that flares in the same direction as the direction in which said propagation axis extends so as to reduce the speed of said syngas/plasma jet mixture, and so as to optimize injection of said fluid;
  • the feed enclosure and the reactor are provided with injection orifices for injecting a protective fluid, which orifices are connected to an injection circuit for injecting said fluid;
  • the inlet port has a feed orifice for feeding in said syngas whose diameter D is such that D/d is greater than or equal to 10;
  • this ratio between the diameter of the feed orifice and the diameter of the plasma jet makes it possible to avoid head loss at the interface between the inlet port and the internal volume of the feed enclosure. It is thus possible to avoid putting the syngas under pressure while it is being fed in, which could result in less good coupling between the syngas and the plasma jet;
  • the diameter d of the plasma jet being 50 mm
  • the diameter D of the feed orifice is 800 mm
  • the outlet port is connected to at least one setting means for setting the outlet gas.
  • the setting means comprise at least one heat exchanger that makes it possible to quench the outlet gas.
  • the disclosed embodiments also provide a system for treating waste or biomass, which system comprises a first treatment stage for treating waste or biomass, which first stage receives said waste or said biomass and generates a syngas, and a second treatment stage coupled to said first stage for the purpose of receiving said syngas.
  • the second stage is constituted by apparatus for treating the syngas as described above.
  • This system makes it possible to produce an outlet gas that is a purified syngas containing a majority of the species H 2 and CO.
  • This syngas purified by non-transferred-arc plasma torch and having a higher calorific value than it had prior to treatment, has a value in use that predestines it advantageously for use in electricity generation, in producing biofuel, or in organic chemistry, e.g. for producing synthetic polymer.
  • the disclosed embodiments therefore also provide a system for generating electrical energy from waste or biomass, said system comprising at last one gas turbine or at least one gas engine.
  • said system for generating electrical energy is equipped with a system for treating waste or biomass as described above.
  • Said at least one gas turbine, or said at least one gas engine is actuated by said outlet gas generated by said system for treating waste or biomass.
  • the disclosed embodiments also provide a system for producing a synthetic fuel or “synfuel” from waste or from biomass, said system comprising at least one catalytic reactor. According to the disclosed embodiments, said system is equipped with a system for treating waste or biomass as described above.
  • said system further comprises a looping circuit connected firstly to said catalytic reactor for the purpose of recovering said residual gaseous product, and secondly to at least one of the elements chosen from the group comprising at least one injector, at least one injection orifice, said plasma torch, and a combination of these elements for the purpose of feeding said gaseous product into said treatment apparatus.
  • Said looping circuit includes a compressor for compressing said residual gaseous product prior to it being fed into said apparatus.
  • This catalytic reactor is preferably a reactor making it possible for the “Fischer-Tropsch” reaction to take place, i.e. hydrocarbons to be produced by causing a mixture comprising at least carbon monoxide and hydrogen to react in the presence of a catalyst.
  • This method is a well-known industrial method that is not described herein.
  • the catalysts used can be of various types and they generally comprise at least one metal chosen from the group comprising iron, cobalt, ruthenium, and vanadium.
  • the metal is typically dispersed over a medium that can comprise a porous mineral material such as an oxide chosen from the group comprising alumina, silica, titanium oxide, zirconium, rare earths, and combinations of these elements.
  • a porous mineral material such as an oxide chosen from the group comprising alumina, silica, titanium oxide, zirconium, rare earths, and combinations of these elements.
  • the catalyst can, in known manner, further comprise one or more activation agents chosen from at least one of the groups I to VII of the periodic table.
  • the catalytic reactor can be a reactor of the bubble column type.
  • FIG. 1 is a perspective view of apparatus for treating a syngas in a particular embodiment of the disclosed embodiments
  • FIG. 2 is a fragmentary section view of the feed enclosure of the apparatus of FIG. 1 ;
  • FIG. 3 is a diagram showing a system for generating electrical energy from waste or biomass, which system incorporates the treatment apparatus of FIG. 1 .
  • FIGS. 1 and 2 show apparatus for treating a syngas in a preferred embodiment of the disclosed embodiments.
  • This apparatus which forms an in-line system, includes a feed enclosure 1 to which a reactor 2 is connected.
  • the feed enclosure 1 and the reactor 2 each have an internal volume defined by walls, which walls are covered, on the inside, with refractory materials that withstand high temperatures, e.g. based on chromium/corundum. These refractory materials make it possible, in particular, to reduce heat losses.
  • the feed enclosure 1 and the reactor 2 which, in this example, are made of metal, are cooled by an external pressurized fluid circuit, the cooling fluid being, for example, demineralized water.
  • the apparatus is designed not to have any cold spots that might constitute zones for condensation of the particles present in the syngas.
  • the feed enclosure 1 includes a non-transferred-arc or “blown arc” plasma torch 3 .
  • This torch 3 is designed to generate a plasma jet 4 having a propagation axis 6 that is substantially collinear with the main axis of the torch 3 .
  • the use of such a torch 3 makes it possible not only to obtain a plasma jet that has a very high temperature, typically lying in the range 2000° C. to 5000° C. as a function of the power of the torch implemented, but also to procure full independence between the internal volume of the feed enclosure 1 and the plasma torch 3 .
  • the feed enclosure 1 therefore has a cooled isolation valve 6 making it possible to isolate the torch 3 from the feed enclosure 1 . It is then possible to work on the torch 3 without exposing the apparatus as a whole to air.
  • the apparatus advantageously includes automatic permutation means for permuting a first transferred-arc torch with a second transferred-arc torch in order to replace a torch that requires maintenance or in order to increase the power of the torch.
  • automatic permutation means can be actuated hydraulically.
  • the feed enclosure 1 is preferably provided with orifices (not shown) through which a protective fluid can be injected. These orifices are connected to an injection circuit for injecting said protective fluid.
  • This circuit can include a compressor for injecting the protective fluid in pressurized form.
  • the injection orifices are directed so that the fluid is injected tangentially to the inside wall of the feed enclosure 1 so as to surround the plasma jet 4 delivered by the torch 3 and so as to prevent the jet from licking said inside wall directly, which would be detrimental to the structural integrity of the feed enclosure.
  • the protective fluid can be a gas at ambient temperature, the gas preferably being the syngas. It can also be constituted by a liquid such as water or oil. When it is oil, it can be constituted by biomass oil, engine oil, or frying oil.
  • the feed enclosure 1 is also provided with an inlet port 7 placed downstream from the plasma torch 3 for the purpose of feeding in the syngas to be treated in the vicinity of the plasma jet 4 .
  • the inlet port 7 which, in this example, is in the form of a bend, is directed in a manner such as to feed in the syngas in a direction that is distinct from the propagation axis 5 of the plasma jet 4 , so as to establish a turbulent mixture zone between the plasma jet and the syngas.
  • This turbulent mixture zone makes it possible to procure intimate mixing between the syngas to be treated and the plasma jet 4 .
  • the syngas is, in this example, fed in perpendicularly to the propagation axis of the plasma jet.
  • the angle formed between the main axis of the bend and the propagation axis 5 of the plasma jet results from computations and experimentations taking account of the parameters of the plasma jet 4 generated by the non-transferred-arc torch 3 and of the flows to be treated (syngas and components for adjusting the composition of said syngas).
  • this angle can lie approximately in the range 90° to 135°.
  • the propagation axis 5 of the plasma jet is directed so as to direct the syngas/plasma jet mixture towards the reactor 2 in which the syngas hosts reactions leading to it being transformed into the outlet gas.
  • Injectors 8 are therefore placed on the feed enclosure 1 for inserting one or more fluids with a view to adjusting the composition of the syngas to be treated.
  • the injectors can be injection nozzles for injecting a gas such as CO 2 , or nebulizers when a liquid, such as water, is injected.
  • a gas such as CO 2
  • nebulizers when a liquid, such as water, is injected.
  • a combination of these elements can also be implemented.
  • Said injectors 8 are preferably placed in a manner such as to feed in the materials substantially in the direction of the flow of the syngas/plasma jet mixture.
  • the feed enclosure 1 has a flared segment 9 in its downstream portion, the flared segment being flared in the same direction as the direction in which the plasma jet propagates along its propagation axis 5 , thereby making it possible to reduce the speed of the plasma jet 4 .
  • this flared segment 9 is a nozzle of the blast pipe type.
  • the reactor 2 has a substantially cylindrical elongate shape and, in its downstream portion, is provided with an outlet port 10 for the outlet gas.
  • the cylindrical geometrical shape of the reactor 2 is designed so as advantageously to limit the speed of the syngas/plasma jet mixture at the wall of the reactor 2 , this speed being induced by the speed of the plasma jet at the outlet of the torch 3 (typically 400 meters per second (m/s).
  • Generating a protective film over the wall of the reactor and/or of the feed enclosure by feeding in a protective fluid also makes it possible to reduce the speed of the syngas/plasma jet mixture at said walls. It is known that the refractory materials protecting the inside wall of the reactor 2 and of the feed enclosure have low resistance to friction (of about 10 m/s).
  • the longitudinal axis of said reactor 2 is substantially collinear with the propagation axis 5 of the plasma jet so as to limit the contact between the plasma jet and the walls of the reactor 2 .
  • Said reactor 2 constitutes a thermal or thermochemical transformation zone for thermally or thermochemically transforming the syngas to be treated with a view to it being converted into outlet gas. This zone results from the intimate mixing of the syngas to be treated and of the plasma jet that takes place in the feed enclosure 1 .
  • the length of said reactor 2 , or furnace, is determined in order to optimize the residence time of the materials to be synthesized or to be treated, which residence time is necessary for accomplishing the thermochemical reactions.
  • the reactor 2 is also provided with injection orifices for injecting a protective fluid, which orifices are connected to a circuit for injecting said fluid.
  • the reactor 2 In its downstream portion, the reactor 2 preferably has a constriction 11 connected to the outlet port 10 . This constriction makes it possible to accelerate the outlet gas prior to it being extracted via the outlet port 10 .
  • This acceleration makes it possible to obtain a speed that is sufficient to send the outlet gas into a heat exchanger (not shown) connected to the outlet port 10 .
  • This heat exchanger makes it possible to quench the outlet gas and to set the component species of the outlet gas.
  • a duct 12 is placed that is lined with refractory materials.
  • the apparatus is provided with at least one sensor (not shown) for measuring the temperature of the outlet gas in a manner such as to adjust the quality of the outlet gas by adjusting the temperature of the plasma jet 4 coming form the plasma torch 3 .
  • the adjustment of the operating parameters of the plasma torch 3 is technically feasible in a time shorter than one second.
  • the sensor can be an optical pyrometer or a temperature probe mounted on the wall of the duct 12 .
  • the feed enclosure 1 and the reactor 2 can have coupling pieces respectively at the inlet port 7 and at the outlet port 10 making it possible to mount said apparatus onto a more complex system such as a system for treating waste or biomass, or for generating electrical energy from waste or from biomass ( FIG. 3 ).
  • These coupling pieces have shapes chosen from the group comprising a rectangular shape and a cylindrical shape.
  • FIG. 3 is a diagram showing a system for generating electricity from waste or from biomass in a particular embodiment of the disclosed embodiments.
  • This system includes a first stage 13 for treating waste or biomass.
  • the first stage receives waste or biomass at its inlet and generates syngas at its outlet.
  • This stage can, in a known manner, be an autothermal gasification reactor or a single-stage gasification reactor using thermal plasma.
  • the syngas is sent to treatment apparatus 14 for treating the syngas as described above, which apparatus makes it possible to produce an outlet gas.
  • the gas has a temperature lying in the range 1150° C. to 1300° C.
  • the outlet gas is sent to a first heat exchanger 15 for the purpose of setting the gas and of cooling it to a temperature lying in the range 400° C. to 600° C.
  • the outlet gas treated in this way is then sent to a second heat exchanger 16 , at the outlet of which its temperature is in the vicinity of in the range 100° C. to 200° C.
  • the outlet gas then enters a dust collection unit 17 making it possible to collect the particles before the gas is sent into a bag filter 18 .
  • a gas scrubber 19 that makes it possible to solubilize a gaseous pollutant in a liquid is implemented for removing, in particular, any traces of sulfur dioxide or of chlorine.
  • a compressor 20 makes it possible to put the outlet gas treated in this way under extra pressure on a gas turbine 21 .
  • the outlet gas actuates the gas turbine 21 which is connected to an alternator 22 which transforms the mechanical energy into electrical energy.
  • the gas turbine 21 can be replaced merely by a gas engine if the flow rate of the outlet gas is not sufficiently high.
  • the system since the gas turbine (or the gas engine) generates an exhaust gas, the system includes a looping circuit 23 connected firstly to said gas turbine (or to said gas engine) for the purpose of recovering the exhaust gas, and secondly to at least one of the elements chosen from the group comprising at least one injector, at least one injection orifice, the plasma torch, and a combination of these elements, for the purpose of feeding the exhaust gas into the treatment apparatus 14 .
  • the looping circuit 23 also includes a compressor (not shown) for compressing the exhaust gas before it is fed into the apparatus.
  • the exhaust gas is typically carbon dioxide.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Inorganic Chemistry (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Processing Of Solid Wastes (AREA)
US11/870,040 2007-09-21 2007-10-11 Method and apparatus for treating a syngas Abandoned US20090077887A1 (en)

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US13/369,018 US8974555B2 (en) 2007-09-21 2012-02-08 Method and apparatus for treating a syngas

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FR0757777A FR2921384B1 (fr) 2007-09-21 2007-09-21 Procede et dispositif de traitement d'un gaz de synthese
FR0757777 2007-09-21

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WO2009139894A1 (en) 2008-05-15 2009-11-19 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20090307974A1 (en) * 2008-06-14 2009-12-17 Dighe Shyam V System and process for reduction of greenhouse gas and conversion of biomass
WO2012150871A1 (en) 2011-05-03 2012-11-08 FRÂNCU, Bogdan-Sabin Procedure and installation for plasma heat treatment of a gas mixture
CN103127895A (zh) * 2011-12-01 2013-06-05 北京低碳清洁能源研究所 一种具有中空阴极的多段等离子体裂解碳质材料反应器系统
US20130326952A1 (en) * 2010-09-24 2013-12-12 James C. Juranitch Renewable Blended Natural Gas and Rock Wool Production from a Plasma-Based System
EP2690162A1 (en) 2012-07-24 2014-01-29 Fundacion Tecnalia Research & Innovation Equipment for treating gases and use of said equipment for treating a synthesis gas contaminated with tars
US8852693B2 (en) 2011-05-19 2014-10-07 Liquipel Ip Llc Coated electronic devices and associated methods
CN104449853A (zh) * 2014-12-09 2015-03-25 中国东方电气集团有限公司 一种新型三段式等离子气化炉
CN104785183A (zh) * 2015-04-13 2015-07-22 神华集团有限责任公司 一种多段等离子体裂解碳质材料反应器系统
WO2016112460A1 (en) * 2015-01-14 2016-07-21 Plasco Energy Group Inc. Plasma-assisted method and system for treating raw syngas comprising tars

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Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009139894A1 (en) 2008-05-15 2009-11-19 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20110162275A1 (en) * 2008-05-15 2011-07-07 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US8430939B2 (en) 2008-05-15 2013-04-30 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US9243197B2 (en) 2008-05-15 2016-01-26 Enersol Power Llc Radiant heat flux enhanced organic material gasification system
US20090307974A1 (en) * 2008-06-14 2009-12-17 Dighe Shyam V System and process for reduction of greenhouse gas and conversion of biomass
US20130326952A1 (en) * 2010-09-24 2013-12-12 James C. Juranitch Renewable Blended Natural Gas and Rock Wool Production from a Plasma-Based System
WO2012150871A1 (en) 2011-05-03 2012-11-08 FRÂNCU, Bogdan-Sabin Procedure and installation for plasma heat treatment of a gas mixture
US8852693B2 (en) 2011-05-19 2014-10-07 Liquipel Ip Llc Coated electronic devices and associated methods
CN103127895A (zh) * 2011-12-01 2013-06-05 北京低碳清洁能源研究所 一种具有中空阴极的多段等离子体裂解碳质材料反应器系统
EP2690162A1 (en) 2012-07-24 2014-01-29 Fundacion Tecnalia Research & Innovation Equipment for treating gases and use of said equipment for treating a synthesis gas contaminated with tars
CN104449853A (zh) * 2014-12-09 2015-03-25 中国东方电气集团有限公司 一种新型三段式等离子气化炉
WO2016112460A1 (en) * 2015-01-14 2016-07-21 Plasco Energy Group Inc. Plasma-assisted method and system for treating raw syngas comprising tars
GB2550767A (en) * 2015-01-14 2017-11-29 Plasco Conversion Tech Inc Plasma-assisted method and system for treating raw syngas comprising tars
US10883059B2 (en) 2015-01-14 2021-01-05 Plasco Conversion Technologies Inc. Plasma-assisted method and system for treating raw syngas comprising tars
GB2550767B (en) * 2015-01-14 2021-07-28 Plasco Conversion Tech Inc Plasma-assisted method and system for treating raw syngas comprising tars
CN104785183A (zh) * 2015-04-13 2015-07-22 神华集团有限责任公司 一种多段等离子体裂解碳质材料反应器系统

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WO2009037339A1 (fr) 2009-03-26
EP2193099B1 (fr) 2017-04-12
PL2193099T3 (pl) 2017-09-29
ES2630427T3 (es) 2017-08-21
CA2698442C (fr) 2015-09-15
FR2921384B1 (fr) 2012-04-06
CA2698442A1 (fr) 2009-03-26
DK2193099T3 (en) 2017-07-24
FR2921384A1 (fr) 2009-03-27
EP2193099A1 (fr) 2010-06-09
PT2193099T (pt) 2017-07-13

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