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
  • C10J3/22—Arrangements or dispositions of valves or flues
  • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
  • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
• • 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
  • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
• • 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
  • C10J2200/152—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
  • 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
  • C10J2300/0916—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
  • C10J2300/0953—Gasifying agents
  • C10J2300/0956—Air or oxygen enriched air
• • 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 relates to the field of gasification of biomass, and more particularly to a fixed bed gasification system used for the conversion of solid organic material (also called biomass), synthesis gas.
• This gas can be burned, for example in an engine, turbine, oven or boiler, which allows to value the heat energy it contains.
• the invention relates in particular to a gasification system of medium size, of the order of a few hundred kW to a few MW.
• the gasification of the biomass consists in decomposing in the presence of a reactive gas (oxygen for example) a solid, for example wood, in order to obtain a gaseous product.
• a reactive gas oxygen for example
• a solid for example wood
• Drying The moisture of the fuel is removed by evaporation. This operation is endothermic, it takes place at a temperature typically between 100 ° C and 160 ° C.
• Pyrolysis Combustible and non-combustible gases are released by dry biomass from 250 ° C. These gases consist of non-condensable vapors (methane, hydrogen, carbon monoxide, carbon dioxide, etc.) and condensable vapors (tars). The residue of this operation called coke is carbon which contains mineral matter.
• Oxidation it takes place in the presence of the reactive gas (air, water vapor, pure oxygen, hydrogen) which conditions the calorific value of the gas at the outlet of the gasifier.
• the optimization of the oxidation zone is essential insofar as a high proportion of tars produced during the pyrolysis is cracked there.
• the use of air as a reactive gas is the most widespread.
• oxidation or partial combustion is the phase that provides the necessary heat for the three phases of the gasification process.
• Coke reacts with water vapor and carbon dioxide, forming hydrogen and carbon monoxide, the main constituents of the fuel gas produced.
• Different technologies have been developed to implement biomass gasification on an industrial scale. The most common technologies are fixed bed gasifiers (or “gasifiers”) and moving bed gasifiers. These are intended for installations with high thermal power (greater than 10 MW) and require a finely ground fuel.
• Fixed bed gasifiers are intended for installations with lower power and can use coarse fuel (eg wood chips).
• Two main categories of fixed-bed gasifiers are distinguished by the relative direction of circulation of biomass and air: countercurrent or co-current.
• a countercurrent gasifier the biomass feed is through the top of the reactor and the air is injected through the bottom of the unit through a grid.
• the coke undergoes a partial combustion which provides the thermal energy necessary for the different stages of the process.
• the gas passes through the reduction and pyrolysis zones and cools down by drying the biomass.
• This type of gasifier produces a lot of tars that must be removed at the outlet of the gasifier in order to use the synthesis gas produced.
• a co-current gasifier In a co-current gasifier, the supply of biomass and oxidizing agent is in the same direction.
• the product gas passes through the hot zone which makes it possible to crack the tars formed during the pyrolysis reaction.
• the product gas thus leaves the reactor at an elevated temperature of the order of 700 ° C.
• the tar content is therefore much lower than in the case of the countercurrent gasifier.
• the existing co-current gasifiers are limited in terms of maximum power, because the injection of oxidizing agent (air, oxygen, water vapor) is at the periphery, which limits the penetration of the gas.
• reagent hereinafter also referred to as "gasifying agent" in the bed, in particular at the level of the reduction zone.
• gasifier is described for example in the patent application WO 2009/020442 (Detes Maden Enerji Ve Cevre Teknoloji Schemeleri Limited Sirket).
• U.S. Patent No. 594,540 discloses a co-current cylindrical gasifier wherein the air inlet is through the top of the cylinder.
• the air supply nozzle has a cone shape, and the air is brought directly into the biomass bed.
• US Pat. No. 4,306,506 (Energy Recovery Research Group) describes a co-current cylindrical gasifier comprising successively from top to bottom an upper drying zone, then a distillation zone (pyrolysis), then an oxidation zone, and finally a reduction zone.
• the air is introduced through a conduit opening into the "core" of the oxidation zone and having a deflection cone that sends air upwards and downwards from the entire oxidation zone.
• air can also be sent down the reduction zone, this air being primarily intended to cool the reduction zone.
• the air injection causes two drawbacks: on the one hand, the oxygen of the air reacts with the hydrogen of the synthesis gas produced, which reduces the calorific value of the synthesis gas, and On the other hand, the synthesis gas is diluted by the nitrogen present in the air.
• US Patent 4,568,271 discloses a gasifier for the gasification of liquid effluents containing organic compounds.
• the liquids are introduced into a vertical cylindrical container through a pipe located in the top of the gasifier.
• An incandescent bed containing carbon-rich materials is located in the bottom of the cylindrical container.
• Oxygen is introduced into the incandescent bed by a central pipe placed in the bottom of the cylindrical container and then by a cone having openings and located in the incandescent bed.
• Liquid effluents are vaporized and "cracked". This device is only suitable for the treatment of liquid effluents.
• Patent Application DE 10 2010 033 646 discloses a co-current fixed bed gasifier having a "separate" oxidation chamber placed inside the body of the gasifier.
• This oxidation chamber has a conical upper zone with the broad part of the cone at the bottom, an oxidizing agent (air) inlet is provided in the upper part of the oxidation chamber.
• the conical upper zone also comprises a double wall inside which the pyrolysis gases produced in the pyrolysis zone are conveyed and introduced into the oxidation chamber. These pyrolysis gases pass through a grid located on the periphery of the oxidation chamber.
• the oxidation chamber described in DE 10 2010 033 646 typically has a burner arrangement. This device is of complex construction, moreover the pyrolysis gases are very charged in tars, and the intake grid may be quickly obstructed.
• Patent application NL 8200417 (TAB BV) describes a co-current fixed bed gasifier capable of treating a wide variety of fuels.
• This gasifier has an air inlet in the upper body of the gasifier, the air being supplied by a rod in a chamber having an upper conical portion with the wide portion of the cone at the bottom. Due to the shape of the chamber, the diffusion of air into the biomass is not optimal.
• the fixed-bed and co-current gasifiers according to the state of the art are therefore limited in power.
• There is a need for a fixed-bed and co-current biomass gasification device making it possible to overcome the limitations of the prior art in terms of maximum power, which can operate in particular at a maximum power greater than 500. kW, which allows to obtain a synthesis gas with a high yield, a minimum rate of tars, and a minimum ash carbon content.
• a co-current fixed bed gasifier for converting biomass into synthesis gas and ash using a gasifier, said gasifier having a reactor body, said reactor body comprising an upper part and a lower part, in which the biomass gasifier is introduced through an inlet duct located at the top of the upper part of the body of the gasifier, the synthesis gas is evacuated via a gas evacuation duct , and the ashes are discharged into the lower part of the lower part of the reactor body through an ash discharge pipe, and said gasifier comprising, from top to bottom,
• said gasifier comprising means for introducing a gasification agent, such as air or oxygen,
• the gasifier comprises an annular zone in which the synthesis gas is collected before leaving the gasifier by said evacuation duct of the synthesis gas.
• the diffusion cone is located below said biomass inlet duct, embedded in the biomass during operation of said gasifier.
• the diffusion cone has an external diameter d which is between 20% and 60%, and preferably between 30% and 50%, of the value of the internal diameter D of the upper part. of the reactor body.
• the internal angle of the cone is advantageously between 60 ° and 120 °, and preferably between 70 ° and 110 °.
• the gasifier according to the invention further comprises a gasification agent inlet located above the grid but below the oxidation zone.
• the area of said annular zone is three to ten times greater (preferably about four to six times greater, and even more preferably about five times greater) than the area of openings in the grid.
• the gasifier according to the invention can be produced in different sizes and with different thermal powers, but its operation is optimal when its thermal power is between 200 and 5000 kW, preferably between 500 and 2500 kW, and even more preferably between 600 and 2000 kW.
• Another subject of the invention is a biomass gasification process using a gasifier according to the invention, in which
• biomass is introduced through said inlet duct
• the gasification agent is introduced by said diffusion cone and by said injection means located in the oxidation zone of the gasifier,
• the synthesis gases are evacuated by said annular zone and said synthesis gas evacuation pipe, and
• the ashes are evacuated through said grate and the ash outlet duct.
• said gasification agent is also injected through an inlet situated above the grid but below the oxidation zone.
• Figures 1 to 4 show schematically different aspects of a gasifier according to the invention.
• Figures 1, 2 and 4 show a longitudinal section
• Figure 3 shows a top view in horizontal section along the plane A-A.
• FIG. 5a represents the variation of the temperature of the synthesis gas at the outlet of the gasifier (dark curve), and the variation of the temperature of the gas in the upper part of the reactor (clear curve).
• Figure 5b shows the variation of the pressure at the top of the gasifier (clear curve), and the variation of the pressure at the bottom of the gasifier (dark curve). The following marks are used:
• the gasifier 14 (also more generally referred to as a reactor) according to the invention has a generally cylindrical reactor body, said body having an upper portion 22 and a lower portion 23.
• the diameter of the lower portion 23 is larger than that of the upper part 22 because of the presence of an annular zone 11 through which the synthesis gas is evacuated.
• biomass 26 is introduced into the gasifier 14 via the inlet duct 1, typically by means of a worm 2.
• biomass is meant solid organic matter such as wood waste in various forms (platelets, pellets, crushed wood, etc.), agricultural by-products (eg example of the straw), dry residues (sludge) of the treatment plant, and any other organic material that can be treated under the conditions for which the gasifier 14 is designed.
• a rotating arm 3 allows the equalization of the biomass on the available surface.
• FIG. 2 is a simplified representation of the reactor 14 of FIG. 1 and shows schematically the approximate positions of the three reaction zones, namely the pyrolysis zone 16, the oxidation zone 17 and the reduction zone 18, and the drying zone 25.
• the oxidation zone 17 is approximately at the level of the reactive gas inlet 4
• the pyrolysis zone 16 is situated above, above the air diffuser cone 13, and the reduction zone 18 lower, above the lower reactive gas inlet (which is optional) 6.
• the ashes pass through a grid 8 located in the lower part 23 of the body of reactor, and accumulate below said grid 8. They are removed periodically or continuously by a rotating arm 9 (typically a double arm) through an ash discharge conduit 10, as shown in FIG. schematic way on the a figure 3.
• a rotating arm 9 typically a double arm
• the main gasification agent inlet (reactive gas) 4 is located at the mid-height of the bed 15. It consists of a set of pipes or pipes ending in injection means 19, 29, which are typically injection nozzles distributed over the periphery of the body 22 of the reactor 14 and supplied by the ducts 4.
• another inlet of reactive gas is provided in the upper part of the bed 15, by the upper duct 5, terminated by a reactive gas diffuser cone 13.
• the diffuser cone 13 allows a better gas supply reagent of the oxidation zone 17 and an increase in the efficiency of the device.
• the inventors have realized that in order to remove the power limitation of a co-current fixed bed gasifier, it is necessary to allow a reactive gas supply of the entire oxidation zone. More particularly, the inventors have found that the peripheral air injection nozzles are no longer sufficient when the thermal power exceeds about 500 kW. Indeed, the limited penetration depth of the reactive gas in the biomass limits the power that can be obtained, knowing that the maximum thermal power is proportional to the reactor section. From a certain diameter D of the reactor, which corresponds to a power of about 500 kW, it is therefore necessary to improve the injection of reactive gas into the oxidation zone; this extra injection is also beneficial for smaller reactors.
• This problem is solved by the cone 13 fixed in the central part of the gasifier, above the oxidation zone, which allows the supply of reactive gas to the core of the oxidation zone.
• This cone 13 is supplied with reactive gas by a rod 5 placed in the axis of the gasifier.
• This device optimally supplies the reactive gas to the center of the gasifier's oxidation zone, and reaches thermal power reaching 5 MW with air as a reactive gas.
• the diffuser cone 13 is situated below the rotating arm 3 which equalizes the level of the biomass, it is embedded in the biomass 26.
• the reactor 14 in the space 24 inside the cone 13, there is creates an empty solid space delimited at the top by the cone 13 and at the bottom by the angle of slope formed by the biomass 26.
• the cone 13 defines two distinct parts in the gasifier 14: an upper part of the drying and pyrolysis 16 of the biomass 26 and a lower part of oxidation 17 and reduction 18 of coke. Its location is defined to optimize the residence time of the solid in each of these parts. This allows you to work sequentially and maximize the conversion of pyrolysis tars. In fact, in a conventional reactor, the tars are emitted into the pyrolysis zone and cracked in the oxidation zone. In the reactor according to the invention, a part of the tars is oxidized in the cone 13. The biomass being pyrolyzed flows along the wall of the cone 13. The pyrolysis gases fill the zone 24.
• homogeneous oxidation is meant gas phase oxidation. This allows a drastic reduction in the tar concentration of the product gas.
• the tar concentration is greater than 500 mg / Nm 3 of gas produced, whereas with the device according to the invention, it can fall to a value of less than 50 mg / Nm 3 , and even less than 35 mg / Nm 3 .
• the homogeneous oxidation zone 24 located inside the cone 13 is not occupied by the biomass. It can thus be used to start the gasifier by producing a combustion of fossil fuel (natural gas, propane or other) introduced by a device (not shown in the figures) inserted in the rod 5.
• the zone 24 also allows during the stabilized step the gasifier 14 to directly oxidize in air a part of the pyrolysis gas and tars generated in the upper part 16.
• the cone 13 is furthermore a heat exchange device making it possible to supply part of the energy necessary for the drying and pyrolysis of the biomass 26.
• the oxidation reaction is exothermic, whereas the drying and pyrolysis requires a energy supply.
• the energy produced by the oxidation is not usable for drying and / or pyrolysis because the biomass bed is a poor thermal conductor.
• the cone 13 is generally made of steel, which is a good thermal conductor, which makes it possible to recover the energy produced by the oxidation and to transfer it at least partly to the biomass located in the zones of pyrolysis 16 and drying 25.
• the cone 13 advantageously has an external diameter d which is between 20% and 60%, and preferably between 30% and 50%, of the value of the internal diameter D of the upper part 22 of the body reactor; these parameters are shown in FIG. 4.
• the internal angle ⁇ of the cone 13 is advantageously between 60 ° and 120 °, preferably between 70 ° and 110 °. These parameters lead to an optimal shape of the oxidation zone 17. If the cone is more flared, ie if its internal angle a is greater than 120 °, on the one hand the flow of the biomass above the cone is difficult, on the other hand the recirculation of the gas inside the cone is not sufficient to allow good oxidation of the pyrolysis gases.
• the cone is less flared, ie if its internal angle a is less than 60 °, it does not constitute a sufficient obstacle to the flow of the biomass and therefore does not allow to define a pyrolysis zone above the cone, the more it does not allow the recirculation of the pyrolysis gases inside the cone.
• the simultaneous presence in the oxidation zone 17 of the peripheral air inlets 4, 19, 29 and of the central air inlet constituted by the cane and the cone 5, allows a homogeneous air supply of the zone. of oxidation 17, which increases the efficiency of the gasifier 14.
• the presence of the cone 13 further provides an additional zone of oxidation tar in a specific area below the cone.
• the particle concentration of the product gas is higher than in a countercurrent reactor. Indeed, the gas passes through the coke during the reduction phase while its particle size becomes very fine. The gas thus causes part of the coke and ash particles at the outlet of the reactor.
• the problem becomes critical because of the increase in the power provided by the presence of the cone. Therefore, in order to minimize the synthesis gas particle content, it is important to limit the rate of the synthesis gas as it leaves the coke bed in order to reduce the entrainment of the particles.
• Existing devices provide for a gas outlet through the lower gate of the gasifier, they do not reduce the speed of gas extraction, because the size of the grid, and its openings, are necessarily limited to contain the deashing.
• the synthesis gas leaves the reactor 14 by the frustoconical annular zone 11 situated above the grid 8.
• the area of this frustoconical annular zone 11 (defined by the surface the "slope" of biomass above the grid 8 is of the order of three to ten times greater (preferably about four to six times greater, and even more preferably about five times greater) than the area of openings in the 8. This reduces by the same factor the rate of extraction of the synthesis gases with respect to their extraction through the grid 8.
• the device 14 of the present invention allows evacuation of the synthesis gas at low speed so as to to limit particle entrainment because the area of the annular discharge zone 11 is much greater than the openings in the grill e, the gas extraction rate is much lower than it would be by extraction through the grid 8. The entrainment of coke particles and ash is thus very limited.
• the gasifier 14 When the gas extraction is done under the grid, the gas must pass through this very fine solid to pass through the grid, the pressure loss is very important which usually involves installing a high-power extractor on the line of synthesis gas and increases the electrical consumption related to the extraction of gases. In addition, it is also difficult to push the conversion of coke very far because this results in a very fine particle size. The carbon content of the ash therefore remains important which limits the rate of conversion of biomass into syngas.
• the extraction of the gases is above the gate 8, the gases do not have to cross the layer of fine particles. The particle size of the coke can be very fine on the grid 8 without increasing the pressure drop on the synthesis gas line.
• another reactive gas inlet is provided under the grid 8 by the duct 7 which may be an annular duct.
• the duct 7 which may be an annular duct.
• a reactive gas inlet by means of a central tube 6 is provided above the grid 8.
• the injection of reactive gas above the grid 8 makes it possible to extend the Hot zone of the coke towards the bottom of the reactor 14.
• the conversion of the coke is maximized, and the efficiency of the gasifier 14 is further improved.
• An embodiment which has both a reactive gas inlet 7 under the gate 8 and an air inlet 6 opening into the injection holes 27 situated above the gate 8 is illustrated in FIG. 1.
• the additional reagent gas inlets 6.7 allow a significant reduction in the carbon content of the ash, and thus an increase in the overall yield of the gasifier 14.
• the synthesis gas produced by the gasifier 14 according to the invention can be burned or used as a raw material in chemical reactions, such as Fischer-Tropsch synthesis.
• the outer wall of the gasifier 14 according to the invention can be made of steel, and the inner wall, which is in contact with the biomass, of refractory concrete.
• Tests were carried out on a reactor according to FIG. 1 with an internal diameter D of 740 mm and a maximum thermal power of the order of 300 kW.
• the temperatures in the different zones of the reactor were determined under different operating conditions.
• the temperature is of the order of 90 to 120 ° C, in the pyrolysis zone 16 of the order of 250 to 500 ° C, in the oxidation zone 17 of the order of 800 to 1300 ° C, and in the reduction zone 18 of the order of 1100 to 700 ° C.
• the cone 13 has an internal angle of about 80 °.
• the temperature of the synthesis gas and the temperature of the gasifier were measured during the first 15 hours of operation.
• the pressure at the top and bottom of the gasifier was also measured.
• the curves are shown in Figures 5a and 5b.
• the "syngas temperature” is the temperature of the gas produced at the outlet of the gasifier.
• the “reactor temperature” is the temperature of the gas in the upper part of the gasifier.
• Low reactor pressure is the pressure measured at the bottom of the gasifier.
• the “high reactor pressure” is the pressure measured at the top of the gasifier. The difference between these two values indicate the pressure drop of the solid bed traversed by the gas.
• the pressures are indicated in mmCE on the curves. These are in fact negative pressures because the reactor is in slight depression.

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