WO2014193997A1 - Système de pyrolyse et procédé d'extraction d'un composant bio-huile - Google Patents

Système de pyrolyse et procédé d'extraction d'un composant bio-huile Download PDF

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Publication number
WO2014193997A1
WO2014193997A1 PCT/US2014/039853 US2014039853W WO2014193997A1 WO 2014193997 A1 WO2014193997 A1 WO 2014193997A1 US 2014039853 W US2014039853 W US 2014039853W WO 2014193997 A1 WO2014193997 A1 WO 2014193997A1
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Prior art keywords
solvent
bio
oil
oil component
condenser
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PCT/US2014/039853
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English (en)
Inventor
Raymond Belanger
Christopher Churchill
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Tolero Energy LLC
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Tolero Energy LLC
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Priority claimed from US13/907,494 external-priority patent/US10589187B2/en
Priority claimed from US14/046,883 external-priority patent/US20150096879A1/en
Application filed by Tolero Energy LLC filed Critical Tolero Energy LLC
Priority to CA2913180A priority Critical patent/CA2913180A1/fr
Publication of WO2014193997A1 publication Critical patent/WO2014193997A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09F—NATURAL RESINS; FRENCH POLISH; DRYING-OILS; OIL DRYING AGENTS, i.e. SICCATIVES; TURPENTINE
    • C09F1/00—Obtaining purification, or chemical modification of natural resins, e.g. oleo-resins
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • the disclosure herein relates to pyrolysis vapor condensation, and more specifically to bio-oil component extraction in a pyrolysis system.
  • One method for processing bio-oil vapors obtained from a slow pyrolysis process involves quenching the vapors with biodiesel in a single-pass or stage. While this method may operate acceptably for some situations, continually feeding pure biodiesel into a quenching vessel to condense the bio-oil may prove costly for long-duration processes.
  • biodiesel fuel mixtures produced with bio-oil extracted via the single-pass process may have problems passing fuel combustion standards, such as ASTM D975 or D6751.
  • FIG. 1 illustrates a system for extracting bio-oil components from pyrolyzed material .
  • FIG. 2 illustrates a method for condensing bio-oil components from decomposed material fumes.
  • FIG. 3 illustrates further detail for one embodiment of the condensing of FIG. 2.
  • FIG. 4 illustrates one example of a system that employs fast pyrolysis for extracting bio-oil components from pyrolyzed material .
  • FIG. 5 illustrates one embodiment of a fast pyrolizer that may be used in the system of FIG. 4.
  • FIGs. 6A - 6H illustrate various specific embodiments of an elongated tubular housing capable of being used by the fast pyrolizer of FIG. 5.
  • FIG. 7 illustrates a close-up view of section 5-5 of the fast pyrolizer of FIG. 5 that employs an elevator according to one
  • FIG. 8 illustrates a close-up view of section 4-4 of the fast pyrolizer of FIG. 5 that employs a heater according to one embodiment.
  • FIG. 9 illustrates a flow chart for one embodiment of a method of fast pyrolysis.
  • a system that includes a pyrolyzer and a primary condenser.
  • the primary condenser is coupled to the pyrolyzer and includes an input to receive pyrolytic vapors from the pyrolyzer and solvent.
  • the condenser is further configured to condense the pyrolytic vapors by contacting the pyrolytic vapors with the solvent to form a condensed liquid that exits the primary condenser via an output.
  • a capture vessel receives the condensed liquid from the condenser output.
  • a recirculator couples the capture vessel to the primary condenser input and is configured to receive the condensed liquid from the primary condenser, and to provide at least a portion of the condensed liquid as part of or all of the solvent in the primary condenser.
  • Examples further provide for a method of extracting bio-oil components from vapors comprising : (a) pyrolyzing a material ; (b) condensing a first amount of bio-oil component vapors produced by pyrolyzing the material with a solvent to produce a condensed liquid; an (c) recirculating at least a portion of the condensed liquid to condense a second amount of bio-oil component vapors.
  • a non-polar high boiling point solvent is used to quench bio-oil components from a material or waste material pyrolysis vapor stream.
  • the resulting liquid is returned to the quenching zone to quench more pyrolysis vapors and load the solvent with more bio- oil components.
  • an injection rate and temperature of the quenching solution are controlled to obtain a particular quantity and quality of the resulting loaded solution .
  • chemical species such as acetone, acetaldehyde, water and acetic acid may be separated in situ by controlling the temperature.
  • a bio-oil component solution is further concentrated by extracting the solvent mixed with bio-oil components and returning the solvent to the quenching system loop.
  • a small proportion of solvent may be preserved to improve some characteristics like viscosity and solubility, for example, of the final liquid .
  • a liquid is produced from pyrolysis vapors which can be used directly in conjunction with a wide variety of fuels.
  • FIG. 1 illustrates a system, generally designated 100, for extracting bio-oil components from pyrolyzed material.
  • the system 100 includes a pyrolizer 110 where a material 120 is exposed to heat with little or no oxygen present.
  • a pyrolizer 110 where a material 120 is exposed to heat with little or no oxygen present.
  • fast and flash pyrolysis e.g. greater than 1000 °C/min heating rates
  • the material 120 fed to the pyrolizer can consist of and/or contain petroleum compounds, plastics, tires, biomass (both vegetal and animal), solid wastes, extracts of liquid wastes, or a combination thereof, and the like.
  • Gases 112 generated by the pyrolysis of the material 120 are directed from the pyrolyzer 110 to an input of a primary condenser 130.
  • the condenser causes bio-oil component vapor to condense to a liquid form of bio-oil components.
  • the primary condenser takes the form of a quenching chamber. Other embodiments may employ non-quenching techniques.
  • a second input to the condenser receives a condensing solvent 132.
  • the solvent is generally sprayed onto the gases (pyrolysis vapors) to form a bio-oil component/solvent mixture that is stored in a bio-oil component/solvent mixture tank 140.
  • a recirculator 142 couples the inlet to the condenser 130 to an outlet of the mixture tank 140 to feed at least a portion of the bio-oil component/solvent mixture back to the condenser 130.
  • the fed back mixture is then used to quench additional bio-oil component vapors as more fully explained below.
  • a temperature controller 144 may be employed to control the temperature of the mixture going into the condenser to extract an optimal percentage of bio-oil components from the vapor stream .
  • bio-oil component vapors that fail to condense in the primary condenser 130 may be directed to an input of a secondary condenser 134 along a secondary path 136.
  • a condensing process similar to that of the primary condenser 130 is carried out in the secondary condenser 134.
  • a resulting liquid bio-oil component/solvent nnixture from the secondary condenser is fed from an outlet to the nnixture tank 140.
  • a secondary recirculator extends from the mixture tank 140 back to the secondary condenser 134 to feed the bio-oil component/solvent nnixture as the quenching agent in the secondary condenser.
  • the bio-oil component/solvent nnixture tank 140 may maintain a consistent volume, and includes a third outlet that feeds a solvent extraction tank or vessel 150.
  • the solvent component of the bio-oil component/solvent mixture may be separated from the mixture, and returned to the mixture tank 140.
  • the solvent extracted from the mixture can also be returned to the line going from the bio-oil component/solvent mixture tank to the condenser 130.
  • the resulting bio-oil component liquid may then be fed to a solute solution tank 160, where further purification or refining may take place.
  • the characteristics of the condensing solvent can be selected to improve the component separation of the pyrolytic gases 112.
  • the solvent polarity may provide better separation of chemicals of interest, and as such may be selected based on the intended end use.
  • a non-polar or substantially non-polar solvent may be used to capture non-polar chemical species from the bio-oil components which are miscible in standard petroleum fuels.
  • Polar solvents can also be used as the condensing solvent.
  • use of a polar solvent as condensing solvent can cause polar compounds to be trapped, causing the non-polar species to separate in a different layer from the polar solvent. The non-polar species can then be separated .
  • Ionic solvents can also be used and similarly removed, recycled and reused.
  • the primary condenser 130 may further be injected with reagents, such as, for example, steam, hydrogen, or other catalysts. The reagents can be injected into the condenser 130 or blended with the condensing solvent when applicable. The heat present in the pyrolysis vapors or condenser 130 can then be utilized to activate a chemical reaction .
  • the boiling and melting points of the solvent can also be varied .
  • the solvent can be selected to have a melting point lower than that of room temperature to avoid mechanical issues, such as clogging of the condensation and transfer systems.
  • the solvent may also be selected to have a low melting point to avoid freezing during normal ambient storage.
  • the boiling point of the solvent can be selected based on the use of the condenser 130 and solvent, for purpose of condensation .
  • the solvent can further be selected to have a minimum of decomposition during condensation .
  • the solvent can be selected to have a boiling temperature low enough to be distilled under normal or reduced pressure while
  • the solvent can be selected from the following chemical groups; alkanes, alkenes, aromatics, alcohols, ketones, aldehydes, fatty acids, fatty esters, triglycerides, esters, their derivatives, and a combination thereof.
  • the solvent can also include a pure solvent mixture. More complex mixtures like biodiesel, vegetable oil, motor oil, and hydrocarbon distillation cuts can also be used.
  • the solvent can also be ionic liquids some of which can be recycled via atmospheric or vacuum distillation .
  • bio-oil component/solvent solution is formed and contained by the bio-oil component/solvent solution mixture tank 140.
  • component/solvent solution includes components from the gases 112, particularly bio-oil components.
  • the bio-oil component/solvent solution can be captured for a maximum recycling yield as well as minimizing the losses downstream and avoid contamination in the rest of the system .
  • the removal of heat by condensation is obtained when the heat of the gases 112 is transferred to the solvent.
  • this can be accomplished by rapidly contacting the pyrolysis gases 112 with the solvent in the primary condenser 130.
  • the solvent can be sprayed in the direct path of the pyrolysis gases in a quenching process.
  • the solvent may be introduced as a falling film with the gases 112.
  • the bio-oil component/solvent solution contained in the bio-oil component/solvent solution mixture tank 140 is further used as the condensing solvent.
  • the bio-oil component/solvent solution is directed back to the primary condenser 130 via the recirculator 142 as the condensing solvent for further condensation .
  • Examples provide for the system to be operated, among other possibilities, as a batch or a continuous process. In a batch process, the bio-oil component/solvent solution mixture tank 140 is filled with the pure solvent to a level corresponding to the fraction of solvent in the final bio-oil component/solvent solution mixture.
  • a portion of the solvent is transferred to the primary condenser 130 to condense a first portion of bio-oil components.
  • the resulting bio-oil component/solvent solution is continually transferred back to the primary condenser 130 until the liquid level in the bio-oil component/solvent solution mixture tank has reached the filled mark, giving a final bio-oil component/solvent solution mixture with an optimum bio-oil component/solvent ratio.
  • the recirculator is stopped and the final bio-oil component/solvent solution is entirely transferred to solvent extraction tank 150.
  • the bio-oil component/solvent solution may be slowly bled to the solvent extraction tank 150 while fresh or recycled condensing solvent is mixed with the bio-oil component/solvent solution, and this mixture is then introduced to the condensation system.
  • a volume level and concentration of the mixture is kept constant.
  • Embodiments recognize that, after condensation by
  • the embodiment of FIG. 1 includes the secondary condenser 134 to receive a secondary stream from the primary condenser 130 for further condensation. Small quantities of the solvent may be present in the secondary stream 136 where, for example, a solvent has a relatively high boiling point.
  • the solvent can be separated or extracted from the secondary condenser 134 by the solvent extraction system and then returned to the quenching process.
  • the exit temperature of the primary condenser 130 By adjusting the exit temperature of the primary condenser 130 it is possible to selectively extract bio-oil components from the bio-oil component/solvent solution . For example, by controlling a gas outlet exit temperature of the primary condenser 130 to about 125 degrees C, it is possible to remove the acetic acid, water, methanol, and all other light chemical species having a boiling point inferior to the set temperature. This results in an anhydrous bio-oil component/solvent solution containing little organic acids which can be stripped during the solvent recycling step.
  • the condensing solvent can be removed by heating and condensing the vapors either by atmospheric or reduced pressure distillation, evaporation, and flash evaporation, or other methods.
  • the bio-oil component/solvent solution can be cooled or the heat absorbed from the primary condenser 130 can be used beneficially to help in solvent extraction 150.
  • the solvent is then usually, but not necessarily, purified further before being sent back to the primary condenser 130.
  • the solvent can be extracted in its totality, the resulting bio-oil components solution can also contain a fraction of the condensing solvent in order to improve its physicochemical
  • bio-oil component solution or concentrate is chemically and physically stable and can be stored, blended or further processed while maintaining chemical properties.
  • FIG. 2 illustrates a method for using a solvent to obtain bio-oil components from thermally decomposed material fumes. Reference is made to the embodiment of FIG. 1 in describing elements of FIG. 2.
  • a material is thermally decomposed to produce vapors.
  • the vapors may include
  • a pyrolyzer may be used to decompose the material in the absence of oxygen to produce the vapors.
  • the vapors produced in (210) can be obtained by heating the material (e.g. by exposure to a heating rate of 10,000 degrees Celsius/minute) without oxygen so that the material decomposes, producing gases.
  • the vapors are provided to a condenser, such as a quenching reactor.
  • the quenching reactor cools the gases from (210) by, for example, exposure to a quenching solution .
  • quenching reactors include a condenser, such as described in FIG. 1, provided with a solvent.
  • the quenching solution may be a pure solvent (e.g. substantially of a single kind of compound), a mixture of different compounds, or a loaded solvent (e.g . including having been exposed to, and loaded, with bio-oil components as more fully described below in (230) and (240)) .
  • the heated vapors are quenched at (230) by exposure to the quenching solution, and the quenching solution is loaded with bio- oil components from the heated vapors at (240) .
  • the quenching solution, material and condenser may be selected or configured so that particular components are loaded into the solvent. For example, aspects of the steps described above at (210) through (230) can be varied for
  • the injection rate of the solvent and temperature of the quenching solution may be manipulated by the temperature controller to control the quantity and quality of the resulting loaded solution .
  • the temperature can be controlled to separate undesired chemical species.
  • the loaded solvent having bio-oil components is recirculated to further quench vapors.
  • Examples provide for (230)-(250) to be performed, among other possibilities, as a batch or a continuous process.
  • a batch process once a target concentration of chemical species is attained, the loaded solvent is transferred to the solvent extraction tank or system .
  • the loaded solvent is slowly bled to the solvent extraction tank or system while fresh or recycled solvent is mixed with the loaded solvent, and this mixture is then introduced to the quenching system .
  • a level and concentration of the mixture is kept constant.
  • FIG. 3 illustrates further detail for one specific quenching method corresponding to the condensing step 230 described above in FIG. 2.
  • the quenching process involves introducing bio-oil component gases into a quenching reactor, at 302, at a temperature selected between 350-750 degrees. Solvent may then be introduced into the reactor, at 304, at a temperature that may be based on a temperature of captured bio-oil components from the quenching process, more fully explained below. The solvent may then be sprayed or otherwise rapidly drawn into contact with the bio-oil component vapor, at 306. The resulting exchange of heat results in the condensation of a large portion of the bio-oil component vapor to bio-oil components liquid.
  • a resulting temperature of about 125 degrees C results in an optimal extraction of desired bio-oil components liquid from the vapor.
  • a determination is carried out, at 312, as to whether the captured liquid is approximately 125 degrees C. If so, then no temperature adjustments are carried out on newly fed solvent into the quenching reactor. Should the temperature not be approximately 125 degrees C, then a temperature adjustment is made, at 314, to increase the temperature of the solvent (if the resulting captured liquid is less than 125 degrees) or reduce the temperature of the solvent (if the resulting captured liquid is higher than 125 degrees C) .
  • This temperature control mechanism optimizes the volume and quality of bio-oil components liquid extracted during each quenching operation.
  • a material in the form of waste wood was directed into a flash pyrolysis oven where it was rapidly heated at a rate in excess of 10,000 °C/min up to about 500-550 °C.
  • the pyrolysis gases generated were rapidly removed and separated from hot biochars and directed, through a heated duct kept near 500°C, to the quencher. There, the pyrolysis vapors were sprayed-in-flight with a relatively cold mixture of condensed/quenched bio-oil components in undecane.
  • the condensed/quenched resulting liquid dropped into the primary quencher tank and was kept at about 125 °C, while the unquenched chemical species having a boiling point inferior to 125 °C went through the quencher tank to exit to a secondary quencher/condenser for collection .
  • the non-condensable gases were directed to a thermal oxidizer, returned to the process for heat generation, for the generation of other chemicals from catalysts, used elsewhere in the plant operation or transported off plant for other usage.
  • the resulting concentration in the primary quencher tank was maintained at about 50% bio-oil components/undecane.
  • undecane is a pure solvent so its extraction can be done at a single temperature which is better for process control.
  • process uses a pure solvent, no residues are left to accumulate in the system and the final product.
  • diesel mixed with a high percentage of bio-oil components may pass standards mandated by diesel fuel standards such as ASTM D975.
  • FIG. 4 illustrates a system, generally designated 400, that employs fast pyrolysis in an application for extracting bio-oil components. It is but one example of an application for fast pyrolysis.
  • the system 400 includes a pyrolizer 402 where material is exposed to heat with little or no oxygen present.
  • the pyrolized material is then fed to a condenser 404 where, for example, bio oil may be condensed from the gases generated by the pyrolizer.
  • An oil extractor 406 may then extract the condensed bio oil for use as a fuel.
  • the material fed to the pyrolizer 402 may contain petroleum compounds, plastics, tires, biomass (both vegetal and animal), solid wastes, extracts of liquid wastes, or a combination thereof, and the like.
  • the material is usually solid, but can also be or contain liquids.
  • FIG. 5 One specific embodiment of a pyrolysis reactor, or pyrolizer, generally designated 500, is shown in FIG. 5.
  • the pyrolizer includes an elongated hollow tube or reactor 502 formed of metal with a feed inlet 504 and an outlet 506. To minimize complexity, the interior of the tube forms an unobstructed flow path, and includes no moving parts. The flow path includes at least one interior surface 508 that forms a contact surface for material progressing through the tube.
  • the elongated hollow tube, or reactor 502 may be formed from different alloys of stainless steel to avoid oxidation. However, a proper selection will often depend on the mechanical, electrical and magnetic properties of the metal . Carbon steel can also be used.
  • FIGs 6A - 6H Various alternative embodiments for the shape of the elongated reactor 502 are shown in FIGs 6A - 6H.
  • the reactor could basically have any cross-sectional shape, but those offering the best material-surface contact are those with a flat bottom. This optimizes the conduction mode of heating .
  • the opposite wall of the contact surface must also not be placed too far from the material falling through it, in order to take advantage of radiation heating. Square, rectangular, or half-circle reactors are preferable.
  • other cross-sectional shape but those offering the best material-surface contact are those with a flat bottom. This optimizes the conduction mode of heating .
  • the opposite wall of the contact surface must also not be placed too far from the material falling through it, in order to take advantage of radiation heating.
  • Square, rectangular, or half-circle reactors are preferable.
  • other cross-sectional shape but those offering the best material-surface contact are those with a flat bottom. This optimizes the conduction mode of heating .
  • the reactor is a straight tubular element from the feed inlet to the outlet, and shown in FIG. 6A, at 602.
  • the material entering the tube will have a constant acceleration. In other words, the speed of the material sliding through the reactor will constantly increase, until it exits the outlet.
  • FIG. 6B illustrates an alternative tube construction that maintains the rectangular cross section, but curves the tube, at 604. This results in the flowing material decreasing its acceleration, but at a constant speed.
  • FIG. 6C illustrates an embodiment where the tube curves laterally back and forth (zigzagged), at 606, to increase path and residence time, and also to increase the mixing of the material falling through the flow path .
  • plural fixed transverse mixing elements 608 may be employed throughout the length of the tube, as shown in FIG. 6D.
  • FIG.s 6E - 6G illustrate tube constructions that employ a coiled configuration to minimize space, yet maximize surface area contact for pyrolysis. It is possible to twist the tube while maintaining the optimum free-sliding angle for the material to flow through to be optimally thermally treated .
  • the general material properties will help determine the slopes (elevation angle of tube) for optimum spread and speed for thermal treatment.
  • FIG. 6E shows a high coil tube, at 610.
  • gravity is still the main drive force to move the material through the length of the tube.
  • FIG. 6F at 612, a more compact form of the coiled tube is shown that cannot rely on gravity alone to move the material .
  • a mechanical device such as a vibration mechanism or pressure device may be employed to cooperate with gravity in moving the material through the flow path .
  • the tube may be relatively flat, such as that shown in FIG. 6G, at 614.
  • a vibration device is attached to the reactor, a mesh or rough reactor floor will help prevent the substance from flowing back downward to the inlet.
  • a compact coiled reactor can alternatively use an open top, or U-shaped ramp, to rapidly remove the gases generated during thermal treatment.
  • an outer shell surrounding the whole coil may be used .
  • the radiative mode of heat transfer can still be used but only when the coil is with a very low profile. The heat from the coil floor above will serve to heat the material by radiation .
  • an enclosed coil could also have a series of holes along its side walls to rapidly remove the gases in the same manner as the topless ramp.
  • an outer shell 616 may be utilized to contain the gases.
  • reactor width could be reduced along the path of the material falling through . Furthermore, the width reduction would also reduce the overall weight and cost of the reactor.
  • the reactor ramp may also be
  • the joining mechanism is preferred to be non-electrically conductive, with a non-electrically conductive joint.
  • the elongated hollow tube is oriented such that the feed inlet 504 is elevated relative to the outlet 506.
  • the force of gravity directs the material downwardly through the tube.
  • the relative elevation angle may be less than the critical free-sliding angle.
  • an additional driving force such as the vibration or pressure device noted above may be used to assist gravity in drawing the material through the tube.
  • the critical free-sliding angle depends on the characteristics of the material, its density, its weight, particle size, etc. Injection of high velocity oxygen- less gas would help move the organic material through the reactor but would also disturb the material bed and most likely lift if from the bottom, thus breaking the heat conduction efficiency. For this reason, a
  • the angle of the reactor can be fixed for a given process but the system can also incorporate mechanical elements permitting for the reactor angle to be changed for optimization of the process.
  • a pivot 702 may be employed for raising and lowering the tube. While FIG. 7 shows a half- pivot, which enables for easy removal of the ramp, various other shapes may also be employed.
  • a support (not shown) at the other end of the tube keeps the feed inlet at the desired height.
  • FIG. 8 illustrates a close-up view of section 5-5 of FIG. 5, and shows one specific embodiment of a heater 802 that employs strip heater elements 804 that are held against the periphery of the reactor by a removable clip 806.
  • a removable clip instead of a removable clip, permanent mounting materials may be used to secure the heater elements to the tube.
  • multiple heaters are distributed along the length of the reactor to optimize the heating. Heating rods, strips, or other types of Joule or infrared heaters can be attached or be part of the reactor faces. As a minimum, only the contact (bottom) face should be heated. With proper insulation the other faces could reach a temperature sufficient enough to help the fast heating process.
  • Heat transfer fluid i.e. air, combustion gases, syngas, thermal oil, ionic or liquid salts, fluidized solid particulates, etc.
  • Heat transfer fluid can be heated remotely using gas burners or via electrical heating and
  • the fluid may be returned to the heating box to be reheated or discarded appropriately.
  • the reactor ramp could also be heated directly using the Joule heating effect by an electrical current passing through it.
  • the ramp should be completely isolated electrically from all other equipment attached to it, including sensors.
  • the ramp includes more than one electrically insulated section, it is possible to heat each section
  • Induction heating can also be used to heat the reactor.
  • a single induction coil can be placed around a straight reactor. It is also possible to use multiple coils. The multiple coils can be controlled individually by one or more induction generators. A single induction generator can also be used in a switching mode using an internal or external switcher to alternatively turn on and off each coil . In this manner, a smaller induction generator can be used to heat a very long section of reactor.
  • Two spiral induction coils can also be used to heat a spiral reactor. A series of spiral reactors can be heated by a series of spiral coils. As is often the case, standard water cooled induction coils must be thermally insulated from the heated ramp as not to cool down the ramp reactor. However, it is also possible to use wire coils, but in this case there would be advantages to include the heat generated by the current going through the wires by installing them in close physical proximity to the ramp element, inside the insulation layer.
  • construction material for the ramp also offers an added advantage of adding magnetic and electrical hysteresis effects to the standard Eddie current induction heating, increasing the overall induction effect which results in a more efficient heating of the ramp reactor.
  • in the case of pyrolysis of material given a high enough induction current, it is also possible to turn the charred layer on the material being pyrolyzed into a heating device.
  • graphite like material can heat up when submitted to an electrical induction field .
  • Induction heating can also be used to generate heat directly in the bulk of the material particles being pyrolyzed, always in close proximity to the unpyrolyzed material, inducing a very high heating rate, but also high liquid yields. This latest phenomenon can also be extended to other applications, including catalysis, cracking, etc.
  • the rate of heating is important for complete thermal treatment within the time of flight inside the reactor, as well as obtaining maximum liquid yield.
  • a single method for heating the reactor ramp could be used, it could be advantageous to use different heating devices to heat different zones along the path of the ramp reactor.
  • the following is simply one example but many cross features can be used consistent with this idea.
  • a thin section for the first section could be used along with induction heating to have a very rapid heat transfer/generation as fresh and relatively cold material comes in through the ramp reactor entrance, the ramp could then transition to a thicker construction material and be heated using electrical heating strips.
  • the heat generation/transfer in that reactor zone does not need rapid response but a sustained temperature since the material was already preheated in the first zone.
  • the fast thermal treatment apparatus described herein can be used for many different applications, including thermal treatment of solids, liquids and gases. It can be used for drying or evaporation . It can be used as a fast chemical reactor. It can also be used for fast pyrolysis and gasification . It can also be used in many different applications where a control of the atmosphere is necessary.
  • FIG. 9 illustrates high-level steps for a method of pyrolizing a material. Reference is made to the embodiment of FIG. 5 in describing elements of FIG. 9.
  • a fast pyrolysis reactor that includes an feed inlet, an outlet, and internal walls.
  • the reactor inlet is oriented to a non-vertical elevation with respect to the outlet for gravity feed flow, at 904.
  • a user may then feed material into the reactor inlet, at 906.
  • As the material progresses through the reactor it is heated via direct heat transfer between the material and at least one of the internal walls, at 908.
  • the resulting pyrolized material and gases may then be further processed, depending on the application, at 910.

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Abstract

L'invention concerne un système comprenant un pyrolyseur et un premier condenseur. Le premier condenseur est couplé au pyrolyseur et comprend un port d'admission qui reçoit les vapeurs pyrolytiques provenant du pyrolyseur et un solvant. Le condenseur condense les vapeurs pyrolytiques en les mettant en contact avec le solvant et forme ainsi un liquide condensé qui sort du premier condenseur par un port d'évacuation. Une cuve de capture reçoit le liquide condensé sortant du port d'évacuation. Une unité de recyclage couple la cuve de capture au port d'admission du premier condenseur, ladite unité de recyclage recevant le liquide condensé qui sort du premier condenseur et transformant au moins une partie dudit liquide condensé en solvant utilisé dans le premier condenseur. Le solvant issu du mélange bio-huile/solvant est ensuite extrait dans un système d'extraction et renvoyé vers le système de désactivation.
PCT/US2014/039853 2013-05-31 2014-05-28 Système de pyrolyse et procédé d'extraction d'un composant bio-huile Ceased WO2014193997A1 (fr)

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