• 专利附录
  • 专利说明
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    • 专利摘要:
    system and method for roasting biomass. A biomass roasting system is provided which entails a continuous roasting process involving the introduction of biomass particles into a rotating drum having a low oxygen atmosphere. the particles are conveyed through the drum by a stream of heated gas and thereby simultaneously roasting. The gas exiting the drum is recirculated back to a heat source to reheat the gas before it enters the drum again. A biomass roasting method is also provided.
    公开号:BR112013008504B1
    申请号:R112013008504-5
    申请日:2011-10-06
    公开日:2019-09-17
    发明作者:William B. Teal；Richard J. Gobel；Andrew Johnson
    申请人:Teal Sales Incorporated；
    IPC主号:
    专利说明:

    "SYSTEM AND METHOD FOR BIOMASS ROASTING"
    Cross reference to related application [001] This application claims the benefit of the filing date of US provisional patent application No. 61 / 391,442 filed on October 8, 2010 and US patent application No. 13 / 218,230 filed on 25 August 2011, the complete content of which is incorporated herein as a reference for all purposes.
    Fundamentals of the Invention
    Technical Field [002] This disclosure relates to systems and methods for roasting biomass, including in particular, systems and methods for roasting cellulosic biomass.
    Description of the Related Art [003] Roasting of biomass particles is well known and is a process in which the biomass particles are heated in a low oxygen environment. This causes the volatile compounds contained in the particles to be removed by boiling and the cell structure of the particles to be degraded, resulting in partial mass loss and an increase in friability. It also causes a reaction within the remaining cell structure that improves the product's resistance to moisture. Particles subjected to roasting have a higher energy value when measured in terms of thermal energy per unit weight. The degree of roasting of the biomass particles depends on several factors, including the level of heat applied, the length of time the heat is applied, and the conditions of the surrounding gas (especially with respect to the oxygen level).
    [004] Current systems strive to mechanically control the variables of heat, residence time and oxygen levels to obtain consistent roasted particles. Typical mechanisms designed to perform biomass roasting under low oxygen conditions use mechanical means to conduct the particles (such as trays or rotating screws) and apply heat to the
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    2/32 conduction surfaces for the transport of particles to be subjected to roasting. Such mechanisms suffer from a variety of disadvantages, including making it difficult or impossible to scale up capacity. As the demand for roasted biomass increases, the limited capacity of the current mechanisms becomes an issue that impedes the use of such biomass. Consequently, applicants believe that improved methods and systems capable of efficiently producing roasted biomass particles are desirable. These methods and systems must be based on the principles and concepts that allow rigorous process control at the same time that they are achieved in order to meet the growing demand.
    Brief Summary of the Invention [005] Modalities described herein provide biomass roasting systems and methods that are particularly well suited for roasting biomass particles (including, in particular cellulosic biomass particles) of various sizes, efficiently and consistently . The systems and methods are easily scalable to meet a wide variety of industrial needs and provide improved process control with regard to monitoring and adjusting operational parameters to optimize or model the characteristics of the resulting biomass particles subjected to roasting.
    [006] According to one embodiment, a biomass roasting system can be summarized as including an entrance to receive the biomass particles, a drum reactor configured to rotate around its longitudinal axis, the drum reactor that has a plurality of vanes positioned inside it in a plurality of locations along the length of the drum reactor; a heat source located upstream of the drum reactor to heat the gas contained in the system to a temperature sufficient to perform the roasting of the biomass particles during operation; a fan device coupled to the system to create, when the system is in operation, a flow of heated gas through the drum reactor to intermittently transport the biomass particles along the
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    3/32 length of the drum reactor as the biomass particles are lifted by the vanes and poured through the heated gas stream, as the drum rotates; and gas ducts coupled to at least one of the reactor drum, heat source and fan device, to recirculate a portion of the gas that leaves the drum reactor, back to the heat source to reheat the gas for its re-introduction into the drum reactor .
    [007] The heated gas stream directly heats the biomass particles as the gas stream intermittently transports the biomass particles through the drum reactor. The lifter vanes can be configured to regulate the movement of the biomass particles along the drum reactor, in order to influence the retention time of the biomass particles inside the drum reactor. Lifting vanes may include vanes spaced around an inner circumference of the drum reactor at regular or irregular intervals and in at least three locations along the longitudinal length of the drum reactor. The lifting vanes interact with the heated gas flow to classify the biomass particles according to the density and / or size of the particles, by moving the relatively denser particles with respect to particles of similar sizes and relatively larger particles with respect to particles having similar densities, more slowly along the drum reactor.
    The biomass roasting system can also include a hopper located downstream of the drum reactor to collect the biomass particles submitted to roasting that leave the drum reactor and to discharge the biomass particles submitted to roasting from the system. The system can also include ducts to disperse the system's exhaust gas, escaping from the system, with the control valves and dampers, the control valves and dampers positioned to regulate a pressure level inside the system in order to inhibit oxygen infiltration while allowing exhaust gases to leave the system. The duct set can direct the exhaust gas from the system to a remote device for use of the exhaust gas in an auxiliary or supplementary process. The remote device can be, for example, a burner with
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    4/32 figured to use the exhaust gases for the supply of heat through a heat exchanger for the gas that passes through the drum reactor during operation.
    [008] The system may also include, at least, an airtight chamber located between the entrance and the drum reactor to limit the amount of oxygen that enters the system, upon receipt of the biomass particles. The system may further include at least one sealing mechanism between the drum reactor and adjacent structures, the sealing mechanism, including an airtight chamber between the drum reactor and an external environment and the sealing mechanism coupled to a gas source inert or semi-inert for the selective purging of the hermetic chamber during the start or stop operation.
    [009] The heat source for the system can be an electric immersion duct heater, gas-gas heat exchanger, a low oxygen burner or other conventional heat sources, such as, for example, a burner of wood or other residues, which is configured to supply heat indirectly to the gas stream in the biomass roasting system.
    [0010] The biomass roasting system can also include a steam unit coupled to the drum reactor to introduce steam into the drum reactor and contribute to the roasting of the biomass particles. The steam plant can also provide safety by smoothing and cooling the chain's functionality to improve operational safety.
    [0011] The biomass roasting system can also include a control system configured to selectively adjust the speed of the fan device to regulate the speed and volume of gas through the system. The control system can also be configured to selectively adjust the rotation speed of the drum reactor to regulate a residence time of the biomass particles in the drum reactor. The control system can also be configured to selectively adjust the temperature of the gas flow through the system. The control system can be configured to selectively adjust parameters of gas flow through the system, including volume, speed and / or pressure. The system of
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    5/32 control can also be configured to independently control a plurality of operational parameters to regulate a roasting process of the biomass particles, the operational parameters including at least one of the reactor inlet temperature, the outlet temperature of the reactor, average residence time, oxygen content of the heated gas stream and gas flow characteristics. The control system can be configured to continuously or intermittently adjust at least some of the operational parameters during operation to optimize the roasting process or to adapt the characteristics of the resulting biomass particles subjected to roasting.
    [0012] According to one embodiment, a biomass roasting method can be summarized as including a rotating drum reactor, the drum reactor having a plurality of vanes positioned inside it in various positions along the entire longitudinal extension of the drum reactor ; generation of a stream of heated gas through the drum reactor, sufficient to transport the biomass particles intermittently along the length of the drum reactor, and simultaneously roasting the biomass particles as the biomass particles are lifted through the vanes and poured through the heated gas stream while the drum reactor rotates; and recirculating a portion of the gas leaving the drum reactor back to the entrance of the drum reactor through one or more gas ducts.
    [0013] The method may further include selectively varying at least some of a plurality of operational parameters to model the characteristics of the resulting biomass particles subjected to roasting, the operational parameters, including at least one of, a velocity of the heated gas stream that runs through the drum reactor, a flow of the heated gas stream through the drum reactor, the temperature of the heated gas stream through the reactor, a pressure level inside the drum reactor, a rotation speed of the drum reactor, the oxygen content of the heated gas stream, a moisture content of the biomass particles and a rate of introduction of the biomass particles into the area
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    6/32 tor drum. The method may also include varying selectively the residence time of the biomass particles in the drum reactor. The method may also include adjusting the plurality of vanes within the drum reactor in relation to positioning and / or density to regulate the retention time of the biomass particles inside the drum reactor. The method can also include the passage of the biomass particles through the drum reactor at different speeds according to the density and / or size of the particles. The method may also include the discharge of biomass particles submitted to roasting while substantially preventing oxygen from infiltrating the drum reactor. The method may also include establishing a pressure level inside the drum reactor to inhibit oxygen infiltration into the drum reactor. The method may also include routing the exhaust gases to a device away from the drum reactor for the use of the exhaust gas in an auxiliary or supplementary process, such as, for example, use as a fuel for a remote burner.
    [0014] The method may also include the sealing of the drum reactor in relation to the external environment and selectively purging one or more air seals adjacent to the sealing interfaces of the drum reactor with inert or semi-inert gas. The method can also include the passage of biomass particles through the drum reactor at a flow rate of between about 1-50 tonnes per hour, the biomass particles having an energy density of at least 20 gigajoules / ton (GJ / t) after of having been roasted in the drum reactor.
    [0015] The method can also include the drying of the biomass particles in a rotary dryer, conveyor type, or other type of dryer system before introduction into the drum reactor. The drying of the biomass particles in the dryer-type rotary system prior to introduction into the drum reactor may include drying of the biomass particles to have an average moisture content below 20 percent moisture content, on a wet weight basis.
    [0016] The method may also include the establishment of the heated gas stream such that an inlet temperature of the heated gas stream which
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    7/32 entering the drum reactor is at least 260 ° C (500 ° F) such that an outlet temperature of the heated gas stream leaving the drum reactor is at least 205 ° C (400 ° F). The method may also include the discharge of the biomass particles submitted to roasting after a single passage of the biomass particles through the drum reactor, the particle sizes of the biomass particles submitted to the roasting discharged varying by at least 10% while the density of The energy and moisture characteristics of the biomass particles submitted to roasting are relatively consistent regardless of particle size. The method may further include introducing the biomass particles into the drum reactor, the biomass particles with an average size of about 1.02 cm3 (1/16 cubic inch) to about 16.39 cm3 (1 cubic inch) upon entry. The method may also include venting the drum reactor when in a fault condition. The method may also include the introduction of water vapor into the drum reactor to assist in the roasting of the biomass particles. The introduction of steam into the drum reactor may include the production of steam with a boiler ('boiler') that receives heat from a portion of the gas that leaves the drum reactor.
    [0017] Brief Description of the Drawings [0018] Figure 1 is a schematic diagram of a biomass roasting system according to one modality.
    [0019] Figure 2 is a schematic diagram of an integrated biomass processing system according to a modality.
    [0020] Figure 3 is an isometric view of a biomass roasting system according to another modality.
    [0021] Figure 4 is a rear isometric view of the biomass roasting system in Figure 3.
    [0022] Figure 5 is a side elevation view of the biomass roasting system in Figure 3.
    [0023] Figure 6 is a top plan view of the biPetition roasting system 870190066340, from 7/15/2019, p. 17/62
    8/32 omass of Figure 3.
    [0024] Figure 7 is a side elevation view of a drum reactor and adjacent components of the biomass roasting system of Figure 3.
    [0025] Figure 8 is a cross-sectional view of the drum reactor of Figure 7, taken along line 8-8.
    [0026] Figure 9 is a side elevation view of a fence assembly, according to a modality, which is usable with the biomass roasting system of Figure 3.
    [0027] Figure 10 is an enlarged detail view of a portion of the seal assembly of Figure 9.
    [0028] Figure 11 is a cross-sectional view of the seal assembly in Figure 9, taken along line 11-11 in Figure 10.
    Detailed Description of the Invention [0029] In the description presented below, some specific details are presented in order to provide a complete understanding of the various modalities described. However, one usually versed in the relevant technique will recognize that modalities can be practiced without one or more of these specific details. In other cases, well-known structures or steps associated with industrial process equipment and industrial processes may not be shown or described in detail, in order not to unnecessarily confuse the descriptions of the modalities. For example, it will be appreciated by those usually versed in the relevant technique that various sensors (eg temperature sensors, oxygen sensors, etc.), control devices and other industrial process controls can be provided and managed by means of a controller. programmable logic (PLC) or other suitable control system to monitor the biomass roasting systems described here and to control the operational parameters of the roasting processes to optimize or model the characteristics of the resulting biomass particles submitted to roasting.
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    9/32 [0030] Unless the context otherwise requires, throughout the specification and the claims presented below, the word understands and its variations, such as, understanding and understanding must be interpreted in an open, inclusive sense, that is it is, as including, but not limited to ”.
    [0031] In the course of this specification, reference to "a modality" or "modality" means that a particular aspect, structure or characteristic that is described together with the modality is included in at least one modality. Thus, the appearance of phrases of the type "in a modality" or "in a modality" in the course of that specification are not necessarily all referring to the same modality. Furthermore, particular aspects, structures or characteristics can be combined in any suitable way in one or more modalities.
    [0032] As used in this specification and the appended claims, the singular forms one, one, and include the referring plurals, unless otherwise stated. It should also be noted that the term "or" is generally used in its sense, including and / or unless the content clearly dictates otherwise.
    [0033] Figure 1 shows a schematic diagram of a biomass roasting system 10 according to a representative modality. System 10 includes a drum reactor 12 which is supported in order to rotate its longitudinal axis
    16. System 10 also includes an inlet 22 to receive the biomass particles that must be processed, as represented by the arrow marked 24. An airtight chamber or double air seal 26 with optional inert or semi-inert gas purge 27 or similar device is coupled to the inlet 22 to substantially prevent oxygen from entering the system 10. The biomass particles are fed to the system 10. The biomass particles can be fed to the inlet 22 via a conveyor or other conventional transport mechanism of material. In one embodiment, a screw feed conveyor can be used in place of the air seal (s) to create a plug of material that acts as a seal when biomass particles pass through
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    10/32 through entry 22.
    [0034] System 10 further includes a heat source 30 disposed upstream of the reactor drum 12 for supplying heat to a gas stream 34 which is generated within the system 10 by means of a fan device 32, which can be , for example, an induced draft fan device, or a forced draft fan device. The fan device 32 is actuated to pull or force the gas through the reactor drum 12 and circulate the gas (or a substantial part of the gas) back to the heat source 30 to be reheated and supplied to the reactor drum 12 in a manner recirculating. In some embodiments, 80 percent or more of the volume of gas leaving the reactor drum 12 can be recirculated to the intake of the reactor drum 12. In some embodiments, 90 percent or more of the volume of gas leaving the reactor drum 12 is recirculated to the entry of the reactor drum 12. In some embodiments, ninety-five percent or more of the volume of gas leaving the reactor drum 12 is recirculated to the entrance of the reactor drum 12.
    [0035] During the operation, the gas stream 34 acts as a thermal fluid to carry the thermal energy to the biomass particles contained within the drum reactor 12 and provide impulse for the transport of the biomass particles. The gas stream can also heat the internal structure of the drum 12, in particular the lifter vanes, which can also in turn heat the biomass particles. The gas ducts 36 are appropriately sized and coupled to at least the drum reactor 12, heat source 30 and fan device 32 to recirculate the gas stream 34 in the system 10. In some embodiments, a predominant portion or the entire amount of gas entering the reactor drum 12 is recirculated back to the entrance of the reactor drum 12 in a continuous manner while a quantity of the gas generated by the roasting of the biomass particles is expelled or otherwise sent externally to the system 10. In some embodiments , new gas (except for unwanted leakage) is not supplied to the recirculating gas stream 34 during operation.
    [0036] In the illustrated mode, the heat source 30 is in the form of an exchange
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    11/32 gas-gas type heat pain 60. A hot gas stream 35, in the range of about 427 ° C (800 ° F) to about 760 ° C (1400 ° F), for example, is provided to the heat exchanger 60 through an inlet duct 62, as represented by the arrow marked 64. The hot gas stream 35 interacts with the recirculating gas stream 34 of the roasting system 10 to transfer heat thereto. In some embodiments, the heat exchanger 60 is configured to raise the inlet temperature of the roasting gas stream 34 contained in the heat exchanger 60 from about 260 ° C ± 37 ° C (500 ° F ± 100 ° F) up to an outlet temperature of about 371 ° C ± 65 ° C (371 ° C ± 65 ° C (700 ° F ± 150 ° F)). In doing so, the temperature of the other isolated gas stream 35 in the heat exchanger 60 is necessarily lowered before leaving the heat exchanger 60 through an outlet duct 66. The temperature of the other isolated gas stream 35, however, is still insufficiently hot to be useful in other processes; such as, for example, drying of the biomass particles before entering them into the biomass roasting system 10. Therefore, in some embodiments, the gas stream 35 discharged from the heat exchanger 60 through the outlet duct 66 can be routed to a dryer system 70 (Fig. 2), or another device, as represented by the arrow marked 68. In some embodiments, the gas stream 35 discharged can be routed back to the heat exchanger inlet 60 and mixed with another heated gas that has a higher temperature; such as, for example, a remote burner, to adjust the inlet temperature of the heat exchanger 60 to a desirable level or to place it in a desired temperature range.
    [0037] Although the illustrated embodiment of the heat source 30 of Figure 1 is shown as a gas-gas heat exchanger 60 it is understood that other various heat sources 30 can be provided. For example, in some embodiments, an electrical heat source from the immersion can be provided in the path of the gas stream 34 of the biomass roasting system 10. In other embodiments, low oxygen burners can be directed directly inward.
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    12/32 of the system 10 to heat the gas flow 34, without significantly increasing the oxygen level within the system 10. Regardless of the heat source 30, however, it is advantageous to isolate the gas stream 34 in a recirculating form to facilitate the maintenance of an environment with low oxygen level inside the drum reactor 12 that is conducive to the roasting of the biomass particles.
    [0038] At the downstream end of the reactor drum 12, a separation hopper 38 is provided for the collection of biomass particles submitted to roasting (for example, wood chips submitted to roasting, cane bagasse submitted to roasting, other cellulosic biomasses subjected to roasting) as the particles leave the reactor drum 12. These particles are then fed mechanically and / or under the force of gravity to an outlet 40, for collection. One or more hermetic chamber devices 42 are coupled to outlet 40 to substantially prevent oxygen from infiltrating system 10, as particles subjected to roasting are removed from system 10. Smaller particles (for example, fines of wood subjected to roasting, cane bagasse fines subjected to roasting, or other cellulosic biomasses subjected to roasting) that can pass through the separating hopper 38 can be filtered and removed from the gas stream 34 by a filtering device 44, such as a cyclone filtering device. One or more additional hermetic chamber devices 46 can be coupled to a secondary outlet 48 for removing filtered material from system 10 without introducing significant amounts of oxygen into system 10. In some embodiments, a chamber or space between a pair sequentially aligned air seals 42, 46 can be coupled to a source of inert or semi-inert gas for selective purging of the chamber or space; as represented by the arrows marked 43, 47 (Figure 2). In some embodiments, the roasting system 10 may include a cyclone filtering device instead of a hopper 38 to separate and / or filter the biomass particles subjected to roasting from the gas stream 34. In some embodiments, the roasting system 10 may include one or more tire devices
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    13/32 discharge mastics (not shown) to discharge the biomass particles submitted to roasting 10 from the roasting system 10.
    [0039] As previously described, the gas stream 34 is extracted or forced through the reactor drum 12 and returned to the heat source 30 (after the separation of the particles subjected to roasting, chips, fines, dust and / or any debris ), under the influence of the fan device 32. While the substantial majority of the gas is recirculated, some gas can be diverted to the exhaust pipe 50. The gases expelled through the exhaust pipe 50 can be used anywhere in the process or in another process, as represented by the arrow marked 52. For example, the exhaust gas can be used as a fuel to generate heat, to assist the heat source 30 in increasing the temperature of the gas stream 34. The exhaust pipe 50 can include a variable positioning damper 54 which can be used to balance the pressure inside the reactor drum 12 from slightly negative to slightly positive. Depending on the setting, this can be used to inhibit oxygen from entering the system 10.
    [0040] Figure 2 shows a schematic diagram of an integrated biomass processing system 11 according to a representative modality. The integrated biomass processing system 11 includes, among other things, the biomass roasting system 10 described above and a dryer system 70, which is configured to dry the biomass particles prior to introduction into the roasting system 10. In some modalities, the biomass roasting system 10 is configured to receive the biomass particles with a moisture content reduced to 20% below the moisture content, on a wet weight basis, by the dryer system 70. In some modalities, the biomass particles can be wood shavings with an average particle size between about 1.02 cm3 (1/16 cubic inch) to about 16.39 cm3 (1 cubic inch) and having an initial moisture content above 40% in wet weight basis. In some embodiments, the biomass particles may have a substantially consistent size (less than 10% difference), and in other embodiments, the particle size 870190066340, of 7/15/2019, p. 23/62
    14/32 can vary between 10%, 20%, 30% or more.
    [0041] According to the embodiment illustrated in Figure 2, the dryer system 70 includes a rotating drum 71 which is supported so that it can rotate about its longitudinal axis 72. The dryer system 70 also includes an inlet 74 for receiving particles of biomass that must be processed; as represented by the arrow marked 75. The biomass particles can be fed to the inlet 74 via a conveyor or other conventional material transport mechanism.
    [0042] The dryer system 70 is coupled to a burner 76 that is configured to feed a flow of heated gas through the piping 77 through the rotating drum 71 and intermittently carrying the biomass particles through the drum 71, as it spins. The heated gas stream simultaneously dries the biomass particles as the stream drives the particles through the rotating drum 71. Burner 76 can be configured to burn bark and trees, dirty fuels or other types of fuel to heat the gas stream fed to the dryer system 70. The gas stream entering the dryer system 70 can also be supplemented or mixed with other gas streams from the integrated biomass processing system 11, as described in more detail below.
    [0043] At the downstream end of the rotating drum 71, a separating hopper 78 is provided to collect the dried biomass particles (for example, wood chips, dry giant cane chips, other dry cellulosic biomass) as the particles come out of the rotating drum 71. These particles are then fed mechanically and / or under the force of gravity to an outlet 79 for collection, for later use or compaction. Smaller particles and dust (for example, dry wood fines, dry cane fines, other dry cellulosic biomass), which can pass through the separating hopper 78 are filtered and removed from the gas stream through a filtering device 80, such as, for example, a cyclone-type filtering device. These particles are fed to
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    15/32 a secondary outlet 81 for subsequent use or compaction. In some embodiments, the dryer system 70 may include a cyclone-type filtering device in place of a hopper 78 to separate and / or filter dry biomass particles from the gas stream. In some embodiments, the dryer system 70 may include one or more pneumatic discharge devices (not shown) for discharging the dry biomass particles from the dryer system 70.
    [0044] A fan device 92 can be provided to pull or force the gas stream through the rotating drum 71 and route the exhaust gas from the rotating drum 71 to the environmental emissions control equipment 82 to process the exhaust from the dryer system 70 prior to release to the environment, or to other systems, as represented by the arrow marked 83. As an example, the emission control equipment 82 may include a wet electrostatic precipitator (WESP) to facilitate the removal of solid-sized particles submicron and liquid droplets from the exhaust gas stream. Emission control equipment 82 may also include a thermoregenerative oxidizer (RTO) to destroy volatile organic compounds (VOCs) and toxic to the environment that may be present in the exhaust gas. In some embodiments, an RTO can be provided which uses natural gas to heat the exhaust gases to about 815 ° C (1500 ° F), where VOCs are oxidized. In other modalities, the gases extracted from the roasting can be used to heat the RTO which can significantly reduce the operating costs of the RTO since natural gas is otherwise a significant cost in the operation of such equipment.
    [0045] At least a portion of the exhaust from the dryer system 70 can be routed or recycled back to the inlet 74 of the rotating drum 71 and combined with the hot gas stream from the burner 76 to dry the biomass particles, which are continuously fed to the rotating drum 71, as represented by the arrows marked 84. Additional gases from the heat exchanger outlet 60 of the roasting system 10 can also be
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    16/32 combined with the exhaust gases from the dryer system 70 for cleaning before discharge into the environment and / or for introduction back into the dryer system 70, as represented by the arrows marked 85.
    [0046] According to the modality illustrated in Figure 2, the dry biomass particles (for example, dry and fine wood chips) can be sent to another location for further processing, storage or compacting the dry biomass particles as a product individual, as represented by the marked arrow 86. A portion or the complete amount of the dry biomass particles can be sent to the roasting system 10 for further processing, as indicated by the marked arrow 87.
    [0047] As can be seen from Figure 2, the dry biomass particles generated through the dryer system 70 can serve as input material for the roasting system 10. In some embodiments, the dry biomass particles can have a content of average humidity below 20%, on a wet weight basis, when entering the roasting system 10. In other modalities, the average moisture content of the dry biomass particles can be between about 5%, on a wet weight basis, and a moisture content humidity of about 15%, on a wet weight basis. In still other modalities, the average moisture content of the dry biomass particles can be greater than a moisture content of 20%, based on a wet weight.
    [0048] Although dryer system 70 is illustrated as a rotary drum dryer system, such as the one designed and marketed by Teal Sales Incorporated, the signatories of this application, it is noted that other dryer systems can be used in conjunction with modalities of the present invention, including, for example, ovens having screw-type or conveyor-bed conveyor mechanisms. Therefore, modalities of the biomass processing systems described herein are not limited to the specific drying systems illustrated, but can incorporate a wide range of conventional drying systems.
    [0049] Still with reference to Figure 2, the heat source 30 is shown as a
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    17/32 gas-gas heat exchanger 60 which is configured to receive a stream of hot gas from burner 76, as indicated by the arrow marked 88. The stream of hot gas entering the heat exchanger 60 can be mixed with gases from a heat exchanger outlet 60, as represented by the arrows marked 90, to regulate the inlet temperature of the heated gas stream entering the heat exchanger 60. In some embodiments, the inlet temperature of the hot stream gas entering the heat exchanger can be between about 315 ° C (600 ° F) and about 760 ° C (1400 ° F), and in some embodiments, the inlet temperature of the gas stream entering the heat exchanger 60 can be between about 427 ° C (800 ° F) and about 538 ° C (1000 ° F). The gas flow recirculation of the roasting system 10 passes through the heat exchanger 60 and is heated, according to some modalities, to an inlet temperature of the drum reactor of at least 260 ° C (500 ° F). After passing through the reactor drum 12, the heated gas stream has an outlet temperature of the drum reactor of at least 205 ° C (400 ° F). As a result, the biomass particles, which are passed through the roasting drum reactor 12 during operation, are directly subjected to a stream of gas heated to a temperature of at least 205 ° C (400 ° F) throughout the drum reactor length 12. In some embodiments, the inlet temperature of the drum reactor is about 371 ° C ± 65 ° C (371 ° C ± 65 ° C (700 ° F ± 150 ° F)) and the temperature of output of the drum reactor is about 260 ° C ± 37 ° C (500 ° F ± 100 ° F). The inlet temperatures of the drum reactor and the outlet of the drum reactor of the heated gas stream can be monitored with appropriate temperature sensors and controlled using a generic or cascade control circuit to maintain the temperature gradient across the reactor at a desired level during operation.
    [0050] The exhaust gases from the roasting process, which include hydrocarbon compounds separated from the biomass particles by boiling, water vapor and any ambient air that leaks into the system can be enPetition 870190066340, from 07/15 / 2019, p. 27/62
    18/32 walked, according to some modalities, to burner 76 for combustion, as indicated by the arrow marked 91. In this way, the energy contained in the exhaust gases can be used to heat a heat transfer medium for use in the exchanger heat pump 60 to keep the heated gas stream 34 flowing through the barrel reactor 12 at a desired high inlet temperature. Again, in some embodiments, the inlet temperature of the drum reactor can be about that of the drum reactor can be about 371 ° C ± 65 ° C (700 ° F ± 150 ° F) and the outlet temperature of the reactor drum can be about 260 ° C ± 37 ° C (500 ° F ± 100 ° F). The temperature gradient of the drum reactor can be controlled through a cascade control circuit that defines the inlet temperature of the drum reactor. The inlet temperature of the drum reactor can be controlled, for example, by varying the amount of heated gas fed to heat exchanger 60 from burner 76. In some embodiments, burner 76 can be configured to burn bark and trees, dirty fuels or other types of fuels to heat the gas stream 35 fed through the heat exchanger 60. Again heating the gas stream 35 can be supplemented with the combustion of the exhaust gases from the roasting system 10, as represented by the arrow marked 91.
    [0051] Figures 3 to 8 illustrate a biomass roasting system 110 according to another representative modality similar to the biomass roasting systems10 described previously, but with other structural details and a different example of a heat source 130. System 110 includes a drum reactor 112 which is supported on a structural frame 114 to rotate around a horizontal axis of rotation 116. The drum reactor 112 is driven by a motor drive 118, which can be electrically coupled to a control system to selectively control the rotation of the drum reactor 112 and optionally adjust its speed. The control system includes a control panel 120 with appropriate controls (circuit breakers, displays, meters, etc.) to selectively control and monitor the system 110. Other meters and controls (for example, sensors, valves, etc.)
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    19/32 can be located remotely and attached to specific system components for monitoring and control purposes.
    [0052] System 110 also includes an inlet 122, in the form of a hopper for receiving the biomass particles to be processed, as represented by the arrow marked 124. An airtight chamber or double air seal 126 with inert gas purge or semi-inert or similar device is coupled to inlet 122 to substantially prevent oxygen from entering system 110, when biomass particles are introduced. The biomass particles can be fed to the inlet 122 via a conveyor or other conventional material transport mechanism. The flow rate of introduction of the biomass particles can be monitored and controlled to optimize or model the characteristics of the resulting biomass particles submitted to roasting. Stairs 128 or other access devices can be provided so that a user has access to entrance 122 and other components of system 110 for maintenance, monitoring and other purposes.
    [0053] The system 110 also includes a heat source 130 arranged upstream of the drum reactor 112 for supplying heat to a gas stream that is generated in the system 110 by means of a fan device 132, which can be, for example, example, an induced draft fan device or a forced draft fan device. The fan device 132 is driven by a driving motor 134 to pull or force the gas through the drum reactor 112 and circulate it back to the heat source 130 to be reheated and supplied to the drum reactor 112 in a recirculating manner. The gas ducts 136 are appropriately sized and coupled to at least one of, the drum reactor 112, the heat source 130 and the fan device 132, for that purpose.
    [0054] At the downstream end of the drum reactor 112, a separating hopper 138 is provided to separate the biomass particles subjected to roasting from the gas stream, as the particles leave the drum reactor 112.
    These particles are then fed mechanically and / or under the force of graviPetition 870190066340, of 7/15/2019, p. 29/62
    20/32, for an output 140 for collection, for subsequent use or compaction. A hermetic chamber-type device 142 is coupled to outlet 140 to substantially prevent oxygen from infiltrating system 110 as the particles subjected to roasting are removed. Small particles and dust that may pass through the separating hopper 138 are filtered and removed from the gas stream through a filtering device 144, such as, for example, a cyclone-type filtering device. Another hermetic chamber device 146 can be coupled to a secondary outlet 148 to remove filtered material from system 110 without introducing significant amounts of oxygen into system 110. In some embodiments, system 110 may include a cyclone-type filtration device in instead of a hopper 138 to separate and / or filter the biomass particles subjected to roasting from the gas stream passing through the drum reactor 112. In some embodiments, system 110 may include one or more pneumatic discharge devices (not shown) to discharge biomass particles subjected to roasting from system 110.
    [0055] As previously described, the gas flow is pulled or forced through the reactor drum 112 and returned to the heat source 130 (after the separation of the particles subjected to roasting, dust and any debris), under the influence of the fan device 132. Although the substantial majority of the gas is recirculated to the drum reactor 112, part of the gas is diverted to an exhaust chimney 150. The gases expelled through the chimney 150 can be recaptured for use in any other part of the process or by another process, such as, for example, use as a fuel to generate heat. The chimney 150 can include a damper 152 of variable position, which can be used to balance the pressure inside the reactor 112 from slightly negative to slightly positive. Depending on the setting, this can be used to inhibit oxygen from entering system 110.
    [0056] Additional details of the drum reactor 112 will now be described with reference to Figures 7 and 8. As shown in the illustrated embodiment, the drum reactor
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    21/32
    112 is supported in a horizontal orientation over a number of rollers 160. Rollers 160 make contact with drum 112 along bearing tracks 162 which are secured to a circumference of drum 112. The diameter of drum 112 can be 0.9 , 1,2, 1,5 m (3, 4, 5 feet) or more and can be configured to receive and process over 50 tons of biomass particles subjected to roasting per hour.
    [0057] The drive motor 118 is coupled to a belt or drive chain 164 and controlled by means of the control system to selectively rotate the drum 112 at different speeds, such as, for example, about 3 RPM or more or less . High-precision seals 166 are arranged between the rotating drum 112 and the static components to prevent oxygen from infiltrating the system. In this way, seals 166 and other features of the system are able to maintain the gas stream at a consistent low oxygen level by creating a substantially sealed container.
    [0058] Within the drum reactor 112 there are a number of lifter vanes 170 circumferentially spaced in each of a plurality of positions along its longitudinal length. The density of the lifter blades 170 can be designed to satisfy the various needs of the system 110 and can be dependent on numerous interrelated factors, such as, for example, the rotation speed of the drum reactor 112, the flow of material fed to the system. 110, and the speed of the fan device 132 or the strength of the heated gas stream that passes through the drum reactor 112. The vanes 170 are configured to lift the biomass particles, while the drum reactor 112 rotates in the direction indicated by arrow 172 and , then direct and water the biomass particles in the gas stream to be intermittently carried along the length of the 112 reactor drum, predominantly by the kinetic energy of the gas stream, and simultaneously subjected to roasting. This is advantageous in that the transport mechanism for the biomass particles provides a highly efficient means for direct heat transfer.
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    22/32 for particles. Therefore, large quantities of biomass particles can be processed through a system with reduced energy requirements. In addition, the yield or throughput of biomass particles subjected to roasting (tonnes / hour) can be relatively higher when compared to conventional roasting systems of generally comparable sizes.
    [0059] The biomass particles remain in drum 112, for a period of time and are then discharged into the separating hopper 138 or other separation device and sent in the direction indicated by the arrow marked 174 for further handling. A predominant or substantial portion of the gas stream is routed in the direction indicated by the arrow marked 176 and recirculated, heated and reintroduced into the drum reactor 112, as indicated by the arrow marked 178.
    [0060] The system 110 thus allows a continuous roasting process that involves the introduction of biomass particles into a rotating drum reactor 112 through an airtight chamber or chambers 126 to maintain a low level of oxygen inside the roasting system 110 which is beneficial for roasting biomass particles. The particles are transported through the drum 112 by means of the kinetic energy of a stream of heated gas that is generated by the creation of an induced draft or forced draft by means of a fan device 132 connected by a duct 136 to the exit of the drum 112. There is also a heat source 130 upstream of the drum 112, such as, for example, an electric duct heater, of the immersion type (Figure 3) or a gas-gas type heat exchanger (Figure 1). The fan device 132 pulls or forces the gas along the extension or through the heat source 130 and through the drum 112. It is beneficial for the viability of the process, to recirculate the gas that leaves the drum 112, back to the source of heat 130, for reheating. It is also beneficial for the viability of the process, the ability of the heated gas stream to directly heat the biomass particles in an environment of low oxygen content while the gas simultaneously
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    23/32 transports the biomass particles intermittently through the drum reactor 112, as already discussed here.
    [0061] There is naturally a certain flow of gas that is discharged from the 110 system (either to the external environment, or to another component of the related process or not) that is substantially equal to the sum of the gases being removed from the biomass particles due to heating (including water evaporation) and any leakage that may enter the system 110.
    [0062] The inside of the drum 112 contains specialized reeds to control the distance between the lift and the fall 170 that lift and water the particles as the drum 112 rotates, thus exposing the particles to the heated gas stream, causing evaporation of the moisture contained in the particles. As the particles are poured into the drum 112 the movement of the gas inside the drum 112 causes the particles to be transported forward. It usually takes a certain number of rotations for drum 112 to provide sufficient progress in advancing the particles to pass through the entire length of drum 112. The watering and driving process inside drum 112 also classifies the particles. Smaller, lighter particles pass through drum 112 more quickly than larger, heavier particles. This allows the larger particles to remain in drum 112 for a longer residence time and creates a more uniform final product (i.e., large and small particles can be processed together to have similar final characteristics regardless of differences in mass and volume). For example, in some embodiments, the particle size can vary within a particular run of biomass particles subjected to roasting by 10, 20 or 30 percent or more, while the energy density and moisture characteristics of the particles are kept relatively consistent, regardless of particle size. In some embodiments, the reeds 170 can be designed to vary with regard to the location and / or the density of the reeds in different modalities, to influence the residence time of the parts 870190066340, of 7/15/2019, p. 33/62
    24/32 biomass particles inside the 112 drum reactor.
    [0063] When using system 110 to roast biomass particles, heat source 130 is responsible for adding heat to a gas recirculation system within system 110. The heated gas stream within that system gas recirculation in turn directly heats the biomass particles as they are conducted through the 110 system. In this way, the stream of heated gas simultaneously heats directly and transports the biomass particles. This is advantageous in that the transport mechanism for the biomass particles provides a highly efficient means for transferring heat directly to the particles. Consequently, large quantities of biomass particles can be processed by a system with reduced energy requirements. In addition, the yield or throughput of biomass particles subjected to roasting (tons / hour) can be relatively higher when compared to conventional roasting systems of generally comparable sizes. This allows the systems described here to be advantageously implemented, particularly in a commercially viable manner.
    [0064] Elements of the heat source 130 can provide heat through any easily available energy source. In some embodiments, for example, heat can be applied directly to the gas flow through an electrical element (for example, electric duct heater, immersion type 130). In other embodiments, heat can be supplied to the gas stream through a gas-gas 60 heat exchanger (Figures 1 and 2), coupled to a combustion and / or heat dissipation system (for example, the burner 76 of Figures 1 and 2). In another embodiment, low oxygen burners can be directed directly to system 110 to heat the gas stream without significantly increasing the oxygen level within system 110. In some embodiments, the exhaust gas that is discharged from the chimney 150 can be used as part of the process heating fuel. Regardless of the heat source 130, very little additional oxygen is added to system 110 over heating portion 870190066340, from 7/15/2019, pg. 34/62
    25/32 process.
    [0065] The roasting systems and processes are based on the thermal and energetic balance that balances the necessary energy with the process flow, heating source and required residence time. Modalities of the roasting systems and methods described here are particularly well suited to manipulate and control these factors and provide systems and methods that are easily scalable to meet the diverse needs of the industry.
    [0066] For example, the residence time of the particles inside the drum 112 can be controlled by various design and process factors. For example, the speed and size of the fan device 132 can be selected to adjust the speed of the circulation of the heated gas inside the drum 112. In addition, the speed and volume of the heated gas stream can also be adjusted by a damper in the fan inlet of the fan device 132. As another example, the rotation speed of the drum 112 can be adjusted more or less in order to adjust the participation of the lifting and watering effect inside the drum 112, thus creating a time greater or lesser in which the particles remain in suspension. In addition, since the vanes 170 can be designed to operate over a wide range of rotational speeds, the rotational speed of drum 112 can be selectively adjusted using appropriate controls (such as variable speed drive motor) to adjust residence time. In addition, the densification of the vanes 170 within the drum 112 can be used to change the flow conditions within the drum 112 producing an individual scope and inherent shorter or longer residence time. In addition, the size and shape of the vanes 170 can be changed in order to meet the needs of the processed material and to create a less pronounced watering effect, thus impacting the residence time on drum 112.
    [0067] In some modalities, the 170 reeds can be fixed to drum 112 in particular densification and arrangement to optimize or model the characteristics
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    26/32 of the resulting biomass particles submitted to roasting. The length of the drum 112 can also be varied as the project starts to create a longer or shorter residence time. In addition, the loading conditions of the particles can be varied to create greater or lesser resistance to the gas stream inside the drum 112, thus affecting the residence time. For example, in some embodiments, a relatively higher volumetric flow of the biomass particles can be set to fill the interior of drum 112 and slow the progression of the particles through drum 112. On the other hand, a relatively lower volumetric flow of biomass particles it can be configured to reduce stocking inside drum 112 and accelerate the progression of biomass particles through drum 112.
    [0068] The oxygen level inside drum 112 can also be controlled by various design and process factors. For example, the mechanical design of the particle inlet can be selected to include, for example, an airtight chamber, a double airtight chamber with a gas purge, screw mechanisms or the like, with each mechanism having a different level of capacity to prevent oxygen infiltration. Preferably, the amount of oxygen that enters the system 110 together with the particles is minimized, but it is likely to vary with the design according to the particle size and / or the desired production flow of the processed biomass. In addition, the moisture content that enters the particles can be varied in order to control the oxygen level. During processing, the resulting evaporated water partially displaces oxygen within system 110, so the humidity level can be varied to suit production requirements (for example, less initial moisture means less energy required for roasting the particles. , and more initial humidity results in less oxygen in the system). In addition, it is identified that there is an addition of gas to the system, as volatiles and moisture are evaporated from the particles. As previously described, this excess gas can be expelled from the system 110 through a chimney 150 and can, according to
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    27/32 some modalities, be recovered for use in any other part of the process or by another process; such as, for example, use as a fuel to generate heat. The chimney 150 can include a variable position damper 152 that can be used to balance the pressure inside the drum 112 from slightly negative to slightly positive. Depending on the setting of the shock absorber 152, this can be used to inhibit oxygen from entering the system 110.
    [0069] In some modalities, many of the various operational parameters discussed above, as well as other operational parameters, can be adjusted (manually or automatically) during the operation. In other modalities, the operational parameters can be established before the operation. Regardless of the particular control system, the ability to independently control the various operating parameters of the systems described here contributes to particularly versatile biomass roasting systems and methods that are adaptable to changing conditions; for example, the moisture content of the biomass particles selected for processing and a desired energy density of the resulting biomass particles subjected to roasting, which can vary.
    [0070] System 110 can also be fitted with precision seals 166, from swivel to static connections, and other low-infiltration connections and components to provide a particularly well-sealed container to maintain consistently low levels of oxygen within the system 110.
    [0071] Figures 9 to 11 illustrate a representative embodiment of a precision seal assembly 266 that can be used to substantially eliminate oxygen infiltration from the surrounding environment into the drum reactor 212 at a rotational interface. As best shown in Figure 10, the seal assembly 266 can include rigid flange structures 270, which are coupled to a flange 268 of the reactor drum 212 to rotate in unison with it. Flange structures 270 can extend to stationary flange structures 272 positioned upstream of drum 212 relative to the direction of
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    28/32 flow F. A gap or space between stationary flange structures 272 and rotating flange structures 270 can be covered by sealing elements 274 to define an inner chamber 276. This inner chamber 276 can be purged intermittently with inert gas or semi-inert to maintain an inert or semi-inert gas barrier between an environment external to the seal assembly 266 and an internal environment of the drum reactor 212.
    [0072] Sealing elements 274 may include internal reinforcements to provide sufficient stiffness to keep sealing elements 274 in sealing contact with rotating flange structures 270 as drum 212 rotates during operation around the axis of rotation 216 Additional inductive elements 280 can also be provided so as to force one or more of the sealing elements 274 into firm contact with the rotating flange structures 270. In the illustrated embodiment, inductive elements 280 are shown as overlapping spring elements that extend from the stationary flange structures 272 positioned upstream of the drum reactor 212 to a sealing element 274 that overlaps one of the rotating flange structures 270. As shown in Figure 11, the sealing elements 274 can be joined together, from as shown, to prevent wear on the sealing elements 274 as the reactor drum 212 and flange breaks 270 rotate in the R direction during operation.
    [0073] Although each of the flange structures 270, 272 is illustrated as L-shape structural elements, it is noted that the size and shape of the flange structures 270, 272 can vary significantly. Regardless of its size and shape, however, it is advantageous, according to some modalities, to provide an insulated inner chamber 276 that can be selectively purged when necessary (for example, during startup, shutdown or system failure conditions) with gas inert or semi-inert to help maintain an indoor environment inside the 212 drum reactor with a consistently low oxygen level. In addition, regardless of size, shape and configuration
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    29/32 sealing assembly elements 266, a redundant sealing interface is useful to help minimize infiltrations into the internal environment.
    [0074] It is further understood that other seals and sealing devices (for example, hermetic chambers or double hermetic chambers) can be provided at other points that have potential for infiltration into the system, including, for example, in the entrances and exits of the biomass particles . In addition, substantially sealed chambers can also be formed at these locations between the roasting system and the external environment. These chambers can be coupled to sources of inert or semi-inert gas for intermittent purging of chambers with inert or semi-inert gas, such as, for example, during startup, shutdown or during system failure conditions. By purging these chambers, one can advantageously ensure that no or very little oxygen from the surrounding environment infiltrates the recirculation gas in the roasting system. In some modalities, the system can be equipped with double feeding and airtight discharge chambers, which are arranged in series, with the purge with inert or semi-inert gas made possible between the airtight chambers.
    [0075] Various safety devices can also be incorporated in the roasting systems in order to improve operational safety. For example, systems can be equipped with openings that will break or open in the event of a minor explosion or deflagration, of sufficient magnitude to cause damage to the equipment. As another example, spark detection and extinguishing systems can also be integrated into roasting systems, such as, for example, spark detection and extinguishing systems and components marketed by GreCon, Inc. based in Tigard, Oregon. In addition, the operational characteristics of the system can be monitored, for example, by means of various sensors (for example, temperature, pressure, oxygen, etc.), and the obtained operational data can be used to adjust and control the system as necessary to increase safety or to optimize the roasting process. In some embodiments, real-time mass spectroscopy can be
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    30/32 also used to identify compounds in the gas streams and to adjust or control the system as needed, to increase safety and to optimize the roasting process.
    [0076] In some embodiments, steam coming from a boiler separate from a steam plant 93 (figure 2), which is fired by the outlet gas from the reactor drum 12 (as represented by the arrow marked 94) or another fuel or source of Heat can be injected into system 10 (as represented by the arrow marked 95) for additional control of oxygen in the process or as a safe current to suffocate and cool, and can also be used as an inert or semi-inert purge gas in process. In addition, the use of steam as part of the process gas that passes through the drum reactor 12 can also improve the thermal transfer to the biomass particles. In some embodiments, the boiler can be heated by the outlet gas sent to it by piping 96 coupled to the reactor drum 12. In other embodiments, the boiler can be heated by burner 76 or by another heat source. In some embodiments, when in a failure condition, steam may be introduced into the reactor drum 12 in sufficient quantities for the purposes of suffocating and cooling. In this way, the operational safety of the roasting system 10 can be increased.
    [0077] In general, by knowing the processes by which heat, residence time and oxygen levels can be controlled, and by knowing the flexibility through the initial design and the numerous process variables described here, system modalities and biomass roasting methods can be adjusted to adapt to a variety of biomass supplies in a variety of local conditions and provide the necessary flexibility and control to achieve consistent roasting results. In some modalities, for example, roasting systems and methods can be configured to roast biomass particles in the form of wood chips at a minimum flow rate of one ton of biomass particles subjected to roasting per hour, with the resulting biomass particles submitted to
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    31/32 roasting having an energy density of at least 20 GJ / ton.
    [0078] The roasting systems and methods described here are particularly well suited to provide a continuous roasting process that has many advantages over conventional roasting systems, and in particular, in batch systems and methods that require batch processing of biomass particles in a furnace, oven or other similar device. The continuous nature of the roasting systems and methods described here allows, among other things, relatively high throughputs. In addition, the efficiency with which biomass particles can be processed with the systems and methods allows for high material production with relatively lower energy requirements.
    [0079] Although modalities of the roasting systems and methods described herein are illustrated as including reactor drums that revolve around and a horizontally aligned axis of rotation, it is appreciated that in some modalities the axis of rotation can be tilted. In such embodiments, gravity can play a significant role in transporting the biomass particles through the drum reactor. Furthermore, although roasting systems and methods are described here as involving a stream of heated gas that passes through the drum reactor to carry or transport the biomass particles, while simultaneously transmitting heat to the biomass particles to its roasting, it is appreciated that in some modalities the biomass particles can be transported by alternative mechanisms (for example, gravity, screw devices, transport devices, etc.) and subjected to a stream of heated gas flowing countercurrent within of the drum reactor, to roast the biomass particles.
    [0080] In addition, the various modalities described above can be combined to provide additional modalities. These and other changes can be made to the modalities, in the light of the above detailed description. In general, in claims 870190066340, of 7/15/2019, p. 41/62
    In the following sections, the terms used should not be interpreted in a way that limits the claims to the specific modalities disclosed in the specification and the claims, but must be interpreted to include all possible modalities, along with the full scope of equivalent to which such claims qualify.
    权利要求:
    Claims (43)
    [1]
    1. Biomass roasting system, CHARACTERIZED by the fact that it comprises:
    an entrance to receive the biomass particles;
    a drum reactor configured to rotate about an axis of rotation, the drum reactor having a plurality of vanes positioned therein in a plurality of locations along a longitudinal length of the drum reactor, the vanes arranged within the drum at selected positions and density to improve the characteristics of particles resulting from biomass submitted to roasting;
    a heat source upstream of the drum reactor to heat the gas contained in the system to a temperature sufficient to roast the biomass particles during operation;
    a fan device coupled to the system to create, when the system is in operation, a stream of heated gas through the drum reactor sufficient to intermittently transport the biomass particles along the longitudinal length of the drum reactor as the biomass particles are lifted through the reeds and poured through the heated gas stream, while the drum reactor rotates; and gas ducts coupled to at least the drum reactor, heat source and fan device to recirculate at least a portion of the gas leaving the drum reactor back to the heat source to reheat the gas for reintroduction to the drum reactor.
    [2]
    2. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the heated gas stream directly heats the biomass particles as the gas stream intermittently transports the biomass particles through the drum reactor.
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    2/10
    [3]
    3. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the plurality of vanes are configured to regulate the movement of the biomass particles through the drum reactor, in order to influence the retention time of the particles of biomass inside the drum reactor.
    [4]
    4. Biomass roasting system, according to claim 3, CHARACTERIZED by the fact that the plurality of vanes include vanes spaced around an internal circumference of the drum reactor at regular or irregular intervals and in at least three locations along the longitudinal length of the drum reactor.
    [5]
    5. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the plurality of vanes interoperate with the heated gas stream to classify the biomass particles according to the particle densities, through the movement of the particles relatively denser compared to particles of similar dimensions, relatively slower through the drum reactor.
    [6]
    6. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also includes:
    a hopper located downstream of the drum reactor to collect the biomass particles submitted to the roasting that leave the drum reactor and to discharge the biomass particles submitted to the roasting from the system.
    [7]
    7. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    ducts to disperse the exhaust gases from the system;
    control valves; and dampers, control valves and dampers positioned to regulate a pressure level within the system to inhibit oxygen infiltration in the
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    3/10 system while allowing the exhaust gas to exit the system.
    [8]
    8. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    ducts to route the exhaust gas from the system to a remote device for the use of the exhaust gas in an auxiliary or supplementary process.
    [9]
    9. Biomass roasting system, according to claim 8, CHARACTERIZED by the fact that the remote device is a burner configured to use the exhaust gases to generate a heated medium for the supply of heat through a heat exchanger for the gas that passes through the drum reactor during operation.
    [10]
    10. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    at least one airtight chamber coupled between the inlet and the drum reactor to limit the amount of oxygen that enters the system when receiving the biomass particles; and at least one sealing mechanism between the drum reactor and adjacent structures, the sealing mechanism, including a chamber between the drum reactor and an external environment and the sealing mechanism coupled to a source of inert or semi-inert gas for purging camera selection during operation.
    [11]
    11. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the heat source is an electric duct heater of the immersion type positioned upstream of the drum reactor.
    [12]
    12. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the heat source is a heat exchanger positioned upstream of the drum reactor, the heat exchanger configured to transfer heat from a heated gas isolated from the barrel reactor for the gas that passes through the
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    4/10 drum reactor during operation.
    [13]
    13. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the heat source is a low-oxygen burner positioned to directly heat the gas that passes through the drum during operation.
    [14]
    14. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    a steam production plant coupled to the drum reactor to introduce steam into the drum reactor and assist in the roasting of the biomass particles.
    [15]
    15. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    a control system configured to selectively adjust the speed of the fan device to regulate a speed of gas flow through the system.
    [16]
    16. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also includes:
    a control system configured to selectively adjust the rotation speed of the drum reactor to regulate a residence time of the biomass particles in the drum reactor.
    [17]
    17. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    a control system configured to selectively adjust the temperature of the gas flow through the system.
    [18]
    18 Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    a control system configured to selectively adjust the parameters
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    5/10 tracts of gas flow through the system, including volume, speed and / or pressure.
    [19]
    19. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    a control system configured to independently control a plurality of operational parameters to regulate a process of roasting the biomass particles, the operating parameters, including at least one of the reactor inlet temperature, a reactor outlet temperature, a average residence time, oxygen content of the heated gas stream and gas flow characteristics.
    [20]
    20. Biomass roasting system, according to claim 18, CHARACTERIZED by the fact that the control system includes sensors to monitor at least some of the operational parameters and the control system is configured to continuously or intermittently adjust at least some of the operating parameters during operation to optimize the roasting process or to model the characteristics of the resulting biomass particles subjected to roasting.
    [21]
    21. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that the drum reactor is at least 1.5 m in diameter and the system is configured to roast the biomass particles at a minimum rate of one ton of biomass particles submitted to roasting per hour, the biomass particles submitted to roasting having an energy density of at least 20 GJ / ton.
    [22]
    22. Biomass roasting system, according to claim 1, CHARACTERIZED by the fact that it also comprises:
    at least one opening configured to subject the system to an external environment upon deflagration within the drum reactor.
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    6/10
    [23]
    23. Biomass roasting method, CHARACTERIZED by the fact that it comprises:
    rotating a drum reactor about an axis of rotation, the drum reactor having a plurality of vanes positioned therein in each of a plurality of locations along a longitudinal length of the drum reactor;
    generate a stream of heated gas through the drum reactor sufficient to intermittently transport the biomass particles along the longitudinal length of the drum reactor and simultaneously toast the biomass particles while the biomass particles are lifted by the reeds and poured through the stream of heated gas as the drum reactor spins; and recirculating a substantial portion of the gas leaving the drum reactor back to a drum reactor inlet through one or more gas ducts to roast the biomass particles within the drum reactor.
    [24]
    24. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    selectively vary at least some of a plurality of operational parameters to model the characteristics of the resulting biomass particles subjected to roasting, the operating parameters including at least one of the velocity of the gas stream heated through the drum reactor, a volumetric flow of the gas heated through the barrel reactor, a temperature of the heated gas stream through the reactor, a pressure level inside the barrel reactor, a rotation speed of the barrel reactor, the oxygen content of the heated gas stream, a moisture content of the biomass particles and a rate of introduction of biomass particles into the drum reactor.
    [25]
    25. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it also includes:
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    7/10 selectively vary a residence time of the biomass particles in the drum reactor.
    [26]
    26. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    adjust the plurality of vanes within the drum reactor in relation to positioning or density to change the retention time of the biomass particles inside the drum reactor.
    [27]
    27. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    pass the biomass particles through the drum reactor at different speeds according to the density or size of the particles.
    [28]
    28. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    discharge the biomass particles subjected to roasting while substantially preventing the infiltration of oxygen into the drum reactor.
    [29]
    29. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    establish a pressure level inside the drum reactor to inhibit oxygen infiltration in the drum reactor.
    [30]
    30. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it also comprises:
    route the exhaust gas to a remote drum reactor device for use of the exhaust gas in an auxiliary or supplementary process.
    [31]
    31. Biomass roasting method, according to claim 30, CHARACTERIZED by the fact that the routing of the exhaust gas to the remote device of the drum reactor for use of the exhaust gas in the auxiliary process
    Petition 870190066340, of 7/15/2019, p. 49/62
    8/10 air or supplemental includes routing the exhaust gas to a burner configured to use the exhaust gases to generate a heated medium for supplying heat to a gas stream to establish the heated gas stream.
    [32]
    32. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    seal the drum reactor from an external environment, and selectively purge one or more adjacent chambers by sealing the drum reactor interfaces with an inert or semi-inert gas.
    [33]
    33. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it also includes:
    transfer heat from an isolated heated gas from the drum reactor to a gas stream to establish the heated gas stream that passes through the drum reactor during operation.
    [34]
    34. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    passing the biomass particles through the drum reactor at a minimum rate of one ton per hour, the biomass particles having an energy density of at least 20 GJ / ton after being subjected to roasting inside the drum reactor.
    [35]
    35. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    dry the biomass particles in a rotary dryer system before introducing them into the drum reactor.
    [36]
    36. Biomass roasting method according to claim 35, CHARACTERIZED by the fact that the drying of the biomass particles in the rotary type dryer system before introduction into the drum reactor includes drying
    Petition 870190066340, of 7/15/2019, p. 50/62
    9/10 of the biomass particles to have an average moisture content below 20 percent moisture content, on a wet weight basis.
    [37]
    37. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    establish the heated gas stream in such a way that an inlet temperature of the heated gas stream entering the drum reactor is at least 260 ° C.
    [38]
    38. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    establish the heated gas stream such that an outlet temperature of the heated gas stream leaving the drum reactor is at least 205 ° C.
    [39]
    39. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    discharge the biomass particles subjected to roasting after a single passage of the biomass particles through the drum reactor, the sizes of the biomass particles submitted to the roasting discharged varying by at least ten percent while the energy density and moisture characteristics of the particles of biomass subjected to roasting are relatively constant, regardless of particle size.
    [40]
    40. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    introduce the biomass particles into the drum reactor, the biomass particles having an average size of 1.02 cm 3 to 16.39 cm 3 at the entrance.
    [41]
    41. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it also comprises:
    opening of the drum reactor when in a fault condition.
    Petition 870190066340, of 7/15/2019, p. 51/62
    10/10
    [42]
    42. Biomass roasting method, according to claim 23, CHARACTERIZED by the fact that it further comprises:
    introduce steam into the drum reactor to assist in the roasting of the biomass particles.
    [43]
    43. Biomass roasting method, according to claim 42, CHARACTERIZED by the fact that the introduction of steam into the drum reactor includes producing steam with a boiler that receives heat from a portion of a gas that leaves the drum reactor .
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    同族专利:
    公开号 | 公开日
    CN106595250B|2020-05-26|
    SI2625253T1|2021-04-30|
    EP2625253A1|2013-08-14|
    PT2625253T|2021-02-17|
    EA026196B1|2017-03-31|
    US20130228444A1|2013-09-05|
    CN106595250A|2017-04-26|
    US20120159842A1|2012-06-28|
    US8252966B2|2012-08-28|
    US9359556B2|2016-06-07|
    BR112013008504A2|2017-07-25|
    KR101727967B1|2017-04-18|
    AU2011311977A1|2013-04-11|
    CA2812777C|2017-06-20|
    SG189111A1|2013-05-31|
    EP3800234A1|2021-04-07|
    LT2625253T|2021-03-10|
    EP2625253B1|2020-11-25|
    EA201390492A1|2013-09-30|
    DK2625253T3|2021-02-15|
    WO2012048146A1|2012-04-12|
    US8246788B2|2012-08-21|
    CA2812777A1|2012-04-12|
    KR20140035866A|2014-03-24|
    ES2849186T3|2021-08-16|
    US20120085023A1|2012-04-12|
    AU2011311977B2|2015-01-22|
    CL2013000932A1|2013-09-27|
    SG192451A1|2013-08-30|
    TWI577956B|2017-04-11|
    TW201231900A|2012-08-01|
    CN103249818A|2013-08-14|
    PL2625253T3|2021-08-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US2135934A|1937-12-17|1938-11-08|Buffalo Bolt Company|Rotary furnace|
    GB1335319A|1970-12-30|1973-10-24|Sugano K|Rotary kiln incinerator|
    FR2512053B1|1981-08-28|1985-08-02|Armines|PROCESS FOR THE TRANSFORMATION OF WOODEN MATERIAL OF PLANT ORIGIN AND MATERIAL OF WOODEN PLANT TRANSFORMED BY TORREFACTION|
    EP0385514B1|1985-05-24|1992-09-09|Le Clerc de Bussy, Jacques|Method for obtaining torrefied wood, product obtained, and use in the production of energy|
    FR2628003B2|1985-10-11|1992-01-17|Leroux Andre Jean|COMPACT CARBONIZATION-DEHYDRATION-TORREFACTION DEVICE-HEAT USES|
    FR2592758B1|1986-01-10|1988-03-18|Clerc De Bussy Le|PRODUCTION METHOD AND DEVICE FOR HARVESTING A TORREFIABLE WOODY PRODUCT|
    FR2594134B1|1986-02-13|1988-04-08|Clerc De Bussy Le|PROCESS AND APPARATUS FOR GRILLING FOLLOWING THE TORREFACTION OF WET WOOD FRAGMENTS|
    FR2624876B1|1987-12-22|1994-03-11|Technology Exports Ltd|PROCESS AND DEVICE FOR TORREFACTING PLANT MATERIAL|
    US5720232A|1996-07-10|1998-02-24|Meador; William R.|Method and apparatus for recovering constituents from discarded tires|
    US6226889B1|1998-03-19|2001-05-08|Sepradyne Corporation|Continuous rotary vacuum retort apparatus and method of use|
    US5997289A|1998-05-01|1999-12-07|Harper International Corp.|Rotary calciner with mixing flights|
    FR2781180B1|1998-07-17|2000-09-29|Fours Et Bruleurs Rey|WOOD RETIFICATION REACTOR|
    WO2001044405A1|1999-12-14|2001-06-21|Tirenergy Corporation|Processes for pyrolyzing tire shreds and tire pyrolysis systems|
    US20030221363A1|2002-05-21|2003-12-04|Reed Thomas B.|Process and apparatus for making a densified torrefied fuel|
    NL1025027C2|2003-12-15|2005-06-21|Stichting Energie|Method and system for the production of solids from raw materials.|
    CA2482571A1|2004-09-27|2006-03-27|9103-7366 Quebec Inc.|Apparatus for treating lignocellulosic material, and method of treating associated thereto|
    CA2580389A1|2004-09-27|2006-04-06|9103-7366 Quebec Inc.|Process for treating lignocellulosic material, and apparatus for carrying out the same|
    EP1690980A1|2005-02-11|2006-08-16|Agrotechnology and Food Innovations B.V.|Process and apparatus for conversion of biomass|
    FR2882368A1|2005-02-21|2006-08-25|Andreas Anest|ECOLOGICAL CHARCOAL GUARANTEED WITHOUT WOOD|
    US20060280669A1|2005-06-10|2006-12-14|Jones Fred L|Waste conversion process|
    NL1029909C2|2005-09-08|2007-03-09|Stichting Energie|Torrefaction process for treating biomass in order to produce biofuel, carried out at pressure chosen so that liquid water is present in torrefaction reactor|
    NL1030864C2|2006-01-06|2007-07-09|Stichting Energie|Method and device for treating biomass.|
    US7942942B2|2006-05-21|2011-05-17|Paoluccio John A|Method and apparatus for biomass torrefaction, manufacturing a storable fuel from biomass and producing offsets for the combustion products of fossil fuels and a combustible article of manufacture|
    NL1032001C2|2006-06-14|2007-12-17|Torr Coal Technology B V|Preparation by torrefaction of a solid fuel useful as fuel for a coal-fired power plant involves heating a starting composition comprising a secondary recovered fuel material indirectly at specific mass temperature|
    CA2654900C|2006-06-14|2015-10-06|Torr-Coal Technology B.V.|Method for the preparation of solid fuels by means of torrefaction as well as the solid fuels thus obtained and the use of these fuels|
    FR2903177B1|2006-06-29|2013-07-05|Bio 3D Applic|METHOD AND SYSTEM FOR TORREFACTING A BIOMASS LOAD|
    FR2904405B1|2006-07-31|2008-10-31|Inst Francais Du Petrole|PROCESS FOR PREPARING A BIOMASS-CONTAINING LOAD FOR SUBSEQUENT GASIFICATION|
    CN201046949Y|2006-12-13|2008-04-16|北京联合创业建设工程有限公司|Biomass rapid pyrolyzing furnace|
    CN201041457Y|2006-12-30|2008-03-26|王社昌|Material continuous drying machine|
    US20090007484A1|2007-02-23|2009-01-08|Smith David G|Apparatus and process for converting biomass feed materials into reusable carbonaceous and hydrocarbon products|
    WO2008107044A1|2007-03-07|2008-09-12|Dsm Ip Assets B.V.|Process for drying and purifying a particulate cellulose/plastic waste mixture|
    US8449631B2|2007-03-18|2013-05-28|John A. Paoluccio|Method and apparatus for biomass torrefaction using conduction heating|
    ITTO20070438A1|2007-06-19|2008-12-20|Martini Aldo|APPARATUS FOR THE DECOMPOSITION OF VEGETABLE ORGANIC SUBSTANCES AND THE PRODUCTION OF COMBUSTIBLE GAS VIA THERMOCHEMISTRY, AND RELATIVE METHOD|
    US20090077892A1|2007-07-27|2009-03-26|Shulenberger Arthur M|Biomass energy conversion apparatus and method|
    DE102007050895A1|2007-10-24|2009-04-30|Siemens Ag|Off-stream gasification of biomass as a slurry|
    FR2923732B1|2007-11-16|2011-03-04|Nicolas Ugolin|METHOD USING PLASMA-COUPLED SOLAR THERMAL ENERGY TO PRODUCE LIQUID FUEL AND DIHYDROGEN FROM BIOMASS OR FOSSIL CHARCOAL |
    WO2009065841A1|2007-11-20|2009-05-28|Shell Internationale Research Maatschappij B.V.|Process for producing a purified synthesis gas stream|
    FR2924300B1|2007-11-23|2009-12-04|E T I A Evaluation Technologiq|DEVICE FOR THERMALLY TREATING DIVIDED SOLIDS.|
    US20090151253A1|2007-12-17|2009-06-18|Range Fuels, Inc.|Methods and apparatus for producing syngas and alcohols|
    CN201140098Y|2007-12-18|2008-10-29|沈阳铝镁设计研究院|Torrefaction filler process system|
    RU2010144971A|2008-04-03|2012-05-10|Норт Каролина Стейт Юниверсити |AUTO THERMAL AND MOBILE ACTION DEVICES|
    SE532746C2|2008-06-11|2010-03-30|Bio Energy Dev North Ab|Process and apparatus for the production of dry-refined lignocellulosic material|
    US8161663B2|2008-10-03|2012-04-24|Wyssmont Co. Inc.|System and method for drying and torrefaction|
    CA2681282C|2008-10-03|2012-10-16|Wyssmont Co. Inc.|System and method for drying and torrefaction|
    US8669404B2|2008-10-15|2014-03-11|Renewable Fuel Technologies, Inc.|Method for conversion of biomass to biofuel|
    EP2189512A1|2008-11-24|2010-05-26|Sa Cockerill Maintenance Et Ingenierie|Method of roasting biomass and control method thereof|
    EP2373762A1|2008-12-08|2011-10-12|Foxcoal IP B.V.|Process for the production of paper|
    WO2010068773A1|2008-12-10|2010-06-17|Kior Inc.|Process for preparing a fluidizable biomass-catalyst composite material|
    US8276289B2|2009-03-27|2012-10-02|Terra Green Energy, Llc|System and method for preparation of solid biomass by torrefaction|
    US8217212B2|2009-04-01|2012-07-10|Paoluccio John A|Sequencing retort liquid phase torrefication processing apparatus and method|
    DE102009052902A1|2009-04-06|2010-10-14|Uhde Gmbh|Low-temperature pyrolysis of biomass in the fluidized bed for a subsequent entrainment gasification|
    FR2944344B1|2009-04-10|2013-12-27|Inst Francais Du Petrole|ROTATING OVEN FOR THERMAL TREATMENT OF SOLID MATERIALS|
    US20100270505A1|2009-04-22|2010-10-28|Range Fuels, Inc.|Integrated, high-efficiency processes for biomass conversion to synthesis gas|
    US20100270506A1|2009-04-24|2010-10-28|Goetsch Duane A|Two stage process for converting biomass to syngas|
    FR2945033B1|2009-04-30|2011-08-12|Nicolas Ugolin|DEVICE ELEMENTS FOR A PROCESS USING PLASMA-COUPLED SOLAR THERMAL ENERGY TO PRODUCE LIQUID FUEL AND DIHYDROGEN FROM BIOMASS OR FOSSIL CHARCOAL|
    FI20090183A0|2009-05-08|2009-05-08|Markku Olavi Raiko|Process for thermal treatment of biomass in a boiler|
    US8980064B2|2009-05-14|2015-03-17|Laurence Rex Manderson|Pyrolytic process and apparatus for producing biomass char and energy|
    BRPI0903587F1|2009-05-22|2020-12-01|Engenho Nove Engenharia Ambiental Ltda|process for pyrolysis of biomass and solid waste in multiple stages|
    FR2946131B1|2009-05-29|2014-01-10|Inst Francais Du Petrole|METHOD FOR THERMAL TREATMENT OF BIOMASS WITH A SOLID HEAT.|
    US8709112B2|2009-06-09|2014-04-29|Sundrop Fuels, Inc.|Systems and methods for quenching, gas clean up, and ash removal|
    WO2011001410A1|2009-07-02|2011-01-06|Gershon Ben-Tovim|Torrefaction apparatus|
    US8449724B2|2009-08-19|2013-05-28|Andritz Technology And Asset Management Gmbh|Method and system for the torrefaction of lignocellulosic material|
    SE0950639A1|2009-09-07|2011-03-08|Andritz Tech & Asset Man Gmbh|Wood material drying plant with rotary dryer|
    US9340741B2|2009-09-09|2016-05-17|Gas Technology Institute|Biomass torrefaction mill|
    CA2683139A1|2009-10-05|2011-04-05|Mark A. Lowe|Method for hot oil torrifaction of wood chips|
    CA2686099A1|2009-10-05|2011-04-05|Mark A. Lowe|Oil impregnated particulate biomass, methods of manufacture and use thereof|
    FR2952068B1|2009-10-30|2012-09-28|Olivecoal Concept|METHOD FOR MANUFACTURING FUEL BY OLIVE GRANTING TORREFACTION|
    CA2684107A1|2009-11-02|2011-05-02|Mark Anthony Lowe|Production of hybrid energy pellets|
    TW201127492A|2009-11-16|2011-08-16|Uhde Gmbh|Contrivance and process for the production of a fine-grained fuel from solid or pasty energy feedstocks by means of torrefaction and crushing|
    WO2011062488A1|2009-11-18|2011-05-26|Meneba B.V.|Fuels pellets, their preparation and use|
    FI20096362A|2009-12-18|2011-06-19|Vapo Oy|Process for producing gasified fuel in a high temperature gasifier|
    CH702521A2|2010-01-11|2011-07-15|Mark Breiter|Plant for producing gedarrtem wood, charcoal, wood tar, wood vinegar and syngas.|
    FR2955118B1|2010-01-12|2012-05-04|Inst Francais Du Petrole|DIRECT HYDROLIQUEFICATION PROCESS OF BIOMASS COMPRISING TWO STEPS OF HYDROCONVERSION IN A BITTERING BED.|
    PL2348091T3|2010-01-12|2013-04-30|Ifp Energies Now|Direct biomass hydroliquefaction process comprising two ebullated bed hydroconversion steps|
    FR2955175B1|2010-01-14|2014-10-24|Inst Francais Du Petrole|METHOD AND DEVICE FOR TORREFACTING A BIOMASS LOAD|
    US8282694B2|2010-01-15|2012-10-09|Syngas Technology Inc.|Pretreatment of biomass feed for gasification|
    US8518336B2|2010-01-25|2013-08-27|Mid-Atlantic Technology, Research & Innovation Center, Inc.|Cascading planar baffle reactor|
    US20110179701A1|2010-01-27|2011-07-28|G-Energy Technologies, Llc|Torrefaction of ligno-cellulosic biomasses and mixtures|
    US20110179700A1|2010-03-22|2011-07-28|James Russell Monroe|System and Method for Torrefaction and Processing of Biomass|
    CN101957132A|2010-06-08|2011-01-26|广州迪森热能技术股份有限公司|Dying control method of biomass materials|
    US8246788B2|2010-10-08|2012-08-21|Teal Sales Incorporated|Biomass torrefaction system and method|
    EP2592758B1|2011-11-14|2014-06-04|Ericsson Modems SA|Wireless transmission|US10030199B2|2007-11-23|2018-07-24|Bixby Energy Systems, Inc.|Pyrolisis apparatus|
    US8161663B2|2008-10-03|2012-04-24|Wyssmont Co. Inc.|System and method for drying and torrefaction|
    US8276289B2|2009-03-27|2012-10-02|Terra Green Energy, Llc|System and method for preparation of solid biomass by torrefaction|
    US8449724B2|2009-08-19|2013-05-28|Andritz Technology And Asset Management Gmbh|Method and system for the torrefaction of lignocellulosic material|
    US9005400B2|2010-08-30|2015-04-14|Renewable Fuel Technologies, Inc.|Device and method for controlling the conversion of biomass to biofuel|
    US8246788B2|2010-10-08|2012-08-21|Teal Sales Incorporated|Biomass torrefaction system and method|
    US8669405B2|2011-02-11|2014-03-11|Kior, Inc.|Stable bio-oil|
    WO2012145397A1|2011-04-18|2012-10-26|Hm3 Energy, Inc.|A system and process for producing torrefied biomass using a mass flow reactor|
    CA2878479A1|2011-07-07|2013-01-10|Torrefuels Incorporated|System and process for conversion of organic matter into torrefied product|
    US9127227B2|2011-09-16|2015-09-08|Astec, Inc.|Method and apparatus for processing biomass material|
    US9562204B2|2012-09-14|2017-02-07|Astec, Inc.|Method and apparatus for pelletizing blends of biomass materials for use as fuel|
    GB2502157B|2012-05-19|2018-11-07|Redring Xpelair Group Ltd|Rotating Heat Exchanger|
    EP2855643A4|2012-05-25|2016-01-20|Airex En Inc|Method and apparatus for torrefaction of biomass with a cyclonic bed reactor|
    ES2643587T3|2012-10-25|2017-11-23|Astec, Inc.|Method and apparatus for transforming combinations of biomass materials into pads for use as fuel|
    US9175235B2|2012-11-15|2015-11-03|University Of Georgia Research Foundation, Inc.|Torrefaction reduction of coke formation on catalysts used in esterification and cracking of biofuels from pyrolysed lignocellulosic feedstocks|
    WO2014086600A1|2012-12-07|2014-06-12|Qinetiq Limited|Method of operating a pyrolysis system|
    US20140283439A1|2013-03-21|2014-09-25|Syngas Technology, Llc|Pretreatment of Biomass Feed for Gasification|
    EP2789677A1|2013-04-12|2014-10-15|Kymi Baltic Consulting Oü|Torrefaction plant, its operation and maintenance|
    PL404037A1|2013-05-22|2014-11-24|Boneffice Spółka Z Ograniczoną Odpowiedzialnością|Method for conducting the process of the torrefaction of biomass, installation for carrying out the process of the torrefaction of biomass, torrefaced biomass and a method for purifying exhaust gas from the torrefaction process|
    WO2015027042A1|2013-08-22|2015-02-26|Geophia Llc|Natural mobile processing unit|
    FR3015513B1|2013-12-19|2016-01-01|Axens|METHOD OF TORREFACTING A CARBONACEOUS LOAD COMPRISING AN OPTIMIZED DRYING STEP|
    NO2717573T3|2014-04-15|2018-08-25|
    WO2016046580A1|2014-09-23|2016-03-31|Bon Effice Sp. Z O.O.|A device for treating materials; and an assembly, an installation and a method for conducting a torrefaction process|
    US9333538B1|2015-02-26|2016-05-10|American Biocarbon, LLC|Technologies for material separation|
    US10167428B2|2015-06-01|2019-01-01|Central Michigan University|Methods for biomass torrefaction with carbon dioxide capture|
    KR101701228B1|2015-06-15|2017-02-02|한국생산기술연구원|Apparatus for biomass torrefaction and foreign matter removal|
    CN105352334A|2015-12-09|2016-02-24|故城北新建材有限公司|Hot smoke recycling system|
    CN105396526A|2015-12-10|2016-03-16|苏州国环环境检测有限公司|Synthesizing device of donor-acceptor type thiophene-pyridine copolymer|
    CN105694916B|2016-04-22|2018-06-19|扬州大学|A kind of movable-type intelligent exhaust gas self-loopa biomass charing device|
    CN106318418B|2016-09-23|2019-03-15|河南博顿生物科技有限公司|A kind of method that corn stover low-temperature carbonization prepares biomass carbon fuel|
    CN106517321A|2017-01-06|2017-03-22|四川国创成电池材料有限公司|Preparation method for lithium titanate powder|
    CN106636577B|2017-01-10|2018-10-19|菏泽锅炉厂有限公司|Annealing furnace of the burning liquid petroleum gas to heat|
    CN108426444A|2017-02-14|2018-08-21|柏红梅|Curer|
    CN108619997A|2017-03-22|2018-10-09|柏红梅|Furnace body heating device|
    WO2018186806A1|2017-04-06|2018-10-11|National University Of Singapore|An organic waste treatment system|
    CN106979696B|2017-04-07|2019-04-09|萍乡强盛电瓷制造有限公司|A kind of afterheat utilizing system producing electroceramics shuttle kiln|
    WO2019014515A1|2017-07-14|2019-01-17|Vermeer Manufacturing Company|Hydro excavation vacuum apparatus|
    CN107940946A|2017-09-27|2018-04-20|长兴谐达能源科技有限公司|A kind of drying equipment for being used for biology granulation|
    SE541264C2|2017-11-09|2019-05-28|Valmet Oy|Method and system for processing lignocellulose material|
    CN107990741B|2017-11-29|2019-07-19|贺守印|A kind of retort UTILIZATION OF VESIDUAL HEAT IN temperature regulating device and its temperature control method|
    CN108294143A|2017-12-13|2018-07-20|安徽金龙山葛业有限公司|A kind of baking device of kudzu root tea|
    CN108571861A|2018-04-03|2018-09-25|盐城普鲁泰克炭素有限公司|Drying process for Regenevating Waste Activated Carbon|
    CN109122745B|2018-08-31|2020-09-11|安徽省天河食品有限责任公司|Food baking equipment based on intelligent control of Internet of things|
    US11124724B2|2018-12-05|2021-09-21|Hm3 Energy, Inc.|Method for producing a water-resistant, compressed biomass product|
    CN109870022A|2019-01-10|2019-06-11|嘉兴市鹏程磁钢有限公司|A kind of vertical magnet steel sintering furnace improving cooling efficiency|
    KR102005978B1|2019-02-14|2019-10-01|오앤엠 코리아|Energy saving type hybrid torrefaction facility|
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    法律状态:
    2018-09-18| B07A| Application suspended after technical examination (opinion) [chapter 7.1 patent gazette]|
    2019-04-16| B07A| Application suspended after technical examination (opinion) [chapter 7.1 patent gazette]|
    2019-08-27| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2019-09-17| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/10/2011, OBSERVADAS AS CONDICOES LEGAIS. (CO) 20 (VINTE) ANOS CONTADOS A PARTIR DE 06/10/2011, OBSERVADAS AS CONDICOES LEGAIS |
    优先权:
    申请号 | 申请日 | 专利标题
    US39144210P| true| 2010-10-08|2010-10-08|
    US61/391.442|2010-10-08|
    US13/218,230|US8246788B2|2010-10-08|2011-08-25|Biomass torrefaction system and method|
    US13/218,230|2011-08-25|
    PCT/US2011/055153|WO2012048146A1|2010-10-08|2011-10-06|Biomass torrefaction system and method|
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