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    • 专利摘要:
    Heat removal and recovery in biomass pyrolysis These are pyrolysis methods and apparatus that allow effective heat removal, for example when a desired yield or a desired type of biomass needs to be achieved. According to representative methods, the use of a cooling medium (eg water), either as a primary type or as a secondary type of heat removal, allows for greater control of process temperatures, particularly in the reheat where coal, As a solid by-product of pyrolysis, it is burned. the cooling medium may be distributed to one or more locations within the reheat container as above and / or within a fluidized particle dense phase bed of a solid heat carrier (e.g., sand) to better control the heat removal.
    公开号:BR112013021459B1
    申请号:R112013021459-7
    申请日:2012-02-01
    公开日:2019-10-01
    发明作者:Sathit Kulprathipanja；Paolo Palmas；Daniel N. Myers
    申请人:Ensyn Renewables, Inc.；
    IPC主号:
    专利说明:

    HEAT REMOVAL AND RECOVERY IN BIOMASS PYROLYSIS
    PRIORITY STATEMENT
    This order claims priority to U.S. Order No. 13 / 031.701 filed on February 22, 2011, the contents of which are incorporated herein in full by reference.
    FIELD OF THE INVENTION
    This invention relates to pyrolysis methods and apparatus in which a solid heat carrier (eg, sand) is separated from the pyrolysis reactor effluent and cooled by a cooling medium (eg, water) to improve the control of temperature. Cooling with a cooling medium can occur in or above a fluidized bed of the heat carrier, where the solid coal by-product is burned to provide some or all of the heat necessary to conduct pyrolysis.
    DESCRIPTION OF RELATED TECHNIQUE
    Environmental issues in relation to greenhouse gas emissions from the use of fossil fuels have led to an increasing emphasis on renewable energy sources. Wood and other forms of biomass, including agricultural and forest residues are examples of some of the many types of renewable raw materials being considered for the production of liquid fuels. Energy from biomass based on energy crops, such as short-rotation crops, for example, can contribute significantly to the Kyoto Protocol's goals of reducing greenhouse gas (GHG) emissions.
    Pyrolysis is considered a promising route for obtaining liquid fuels, including transport fuel and heating oil, from biomass raw materials. Pyrolysis refers to thermal decomposition in the substantial absence of oxygen (or in the presence of significantly less oxygen than is necessary to complete combustion). Initial attempts to obtain useful oils from biomass pyrolysis have produced predominantly a slate equilibrium product (ie, slow pyrolysis products). In addition to the desired liquid product, approximately equal proportions of non-reactive solids (coal and ash) and non-condensable gases were obtained as unwanted by-products. More recently, however, significantly improved yields of non-equilibrium primary liquids and gases (including valuable chemicals, chemical intermediates, petrochemicals, and fuels) have been obtained from carbonaceous raw materials through rapid (fast or instant) pyrolysis. at the expense of undesirable slow pyrolysis products.
    In general, rapid pyrolysis refers to technologies that involve rapid heat transfer to the biomass raw material, which is kept at a relatively high temperature for a very short period of time. The temperature of the primary pyrolysis products is then rapidly reduced before chemical equilibrium is achieved. Therefore, rapid cooling prevents valuable reaction intermediates, formed by depolymerization and fragmentation of the biomass building blocks, that is, cellulose, hemicellulose, and lignin, from degrading into low-value non-reactive end products. A series of rapid pyrolysis processes are described in US 5,961,786; Canadian Patent Application 536,549; and by Bridgwater, A.V., Biomass Fast Pyrolysis, Review paper BIBLID: 0354-9836, 8 (2004), 2, 21-49. Rapid pyrolysis processes include Rapid Thermal Processing (RTP), in which one uses an inert particulate or a catalytic solid particulate to transport and transfer heat to the raw material. RTP has been commercialized and operated with very favorable yields (55 to 80% by weight, depending on the biomass raw material) of crude pyrolysis oil.
    Therefore, pyrolysis processes, such as RTP, depend on rapid heat transfer from the solid heat carrier, generally in particulate form, to the pyrolysis reactor. Ά combustion of coal, a solid by-product of pyrolysis, represents an important source of the significant heat requirement to conduct the pyrolysis reaction. The integration of effective heat between, and recovery, the pyrolysis reaction and the combustion (or reheater) sections represents a significant objective in terms of improving the overall pyrolysis economy, under operational and equipment capacity restrictions, for a given feedstock. As a result, there is a continuing need in the art for pyrolysis methods that add flexibility in terms of managing substantial combustion heat, transferring it to the pyrolysis reaction mixture, and recovering it for use in other applications.
    SUMMARY OF THE INVENTION
    The present invention is associated with the discovery of pyrolysis methods and devices that allow effective heat removal, for example, when it is necessary to achieve a desired yield. Depending on the pyrolysis load used, processing capacity may become limited, not by the size of the equipment, but by the ability to remove heat from the general system, as needed to operate within the designed temperatures. While some heat removal schemes, such as passing the recycled heat carrier (eg, sand) through a cooler, may be effective in certain circumstances, they may not be applicable to all pyrolysis systems in terms of meeting objectives cost and performance. The methods and apparatus described in this document, which involve the use of a cooling medium, represent generally less expensive alternatives to provide a necessary heat removal. The cooling medium can be used effectively alone or in combination with other types of cooling, for example, a sand cooler.
    Therefore, the cooling medium can act as a primary or secondary type of heat removal, allowing for greater control of process temperatures, and particularly in the reheater where coal, as a solid by-product of pyrolysis, is burned. Associated with the removal of heat, operational flexibility is added in terms of the type of biomass raw material and processing capacity, which are generally limited by a maximum operating temperature instead of the size of the equipment. In particular to the pyrolysis operation, a cooling medium is distributed to one or more locations within the reheater container, thereby cooling this container if a sand cooler is not used (for example, in view of cost considerations) or otherwise, remove excess heat to an insufficient extent. Generally, the reheater container is operated with a fluidized bed of particles from the solid heat carrier, through which a combustion medium containing oxygen is passed, in order to burn the coal and generate some or all of the heat necessary for pyrolysis . The fluidized bed comprises a dense phase bed below a diluted phase of the particles of the solid heat carrier.
    A cooling medium can be sprinkled, for example, on top of a value carrier, such as sand, which resides in the heater as a fluidized bed of particles. In this way, heat is removed, for example, by converting water, as a cooling medium, into steam. Heat consumption advantageously reduces the overall temperature of the reheater and / or allows the pyrolysis unit to operate at a target capacity. The dispensers can be located in several parts to introduce the cooling medium at multiple points, for example, into the bed of the dense phase and / or in the diluted phase, above the dense phase. The introduction of dilute phase of the cooling medium helps to avoid interruptions of the dense phase bed due to the sudden expansion of volume (for example, of water by conversion to steam) in the presence of a relatively high density of solid particles. Such interruptions can lead, in a harmful way, to a drag of solid particles and losses. The introduction of dense phase (for example, directly in an intermediate section of the dense phase bed), on the other hand, provides a direct cooling of the solid particles. This cooling is effective if the introduction is carried out with sufficient control, and at a flow rate of cooling medium, which avoids significant interruptions of the dense phase bed. In some cases, the cooling medium can be introduced at and above the dense phase bed, and even at multiple locations within and above the bed.
    Therefore, the modalities of the invention are directed towards pyrolysis methods which comprise combining biomass and a solid heat carrier (for example, solid particulate that has been heated in a reheater and recycled) to provide a pyrolysis reaction mixture, for example, in a Rapid Thermal Processing (RTP) pyrolysis unit. The reaction mixture can, for example, be formed by mixing the biomass and the solid heat carrier at the bottom, or below, of an upstream pyrolysis reactor. The mixture is then subjected to pyrolysis conditions, including a rapid increase in the temperature of the biomass to a pyrolysis temperature and a relatively short residence time at this temperature, to provide a pyrolysis effluent. The appropriate conditions are usually achieved using an oxygen-free (or oxygen-free) transport gas that elevates the pyrolysis reaction mixture through an upflow pyrolysis reactor. After pyrolysis, the pyrolysis effluent is separated (for example, using a cyclonic separator) into (1) a solid-enriched fraction comprising both a solid coal and a recycled portion of the solid heat carrier and (2) a fraction devoid of solids comprising pyrolysis products. Pyrolysis products include, after cooling, (1) liquid pyrolysis products that are condensed, such as crude pyrolysis oil and valuable chemicals, as well as (2) non-condensable gases, such as H2, CO, CO2, methane , and ethane. The fraction enriched with solids is then placed in contact with a combustion medium containing oxygen (for example, air or nitrogen-enriched air) to burn at least part of the solid coal and reheat the recycled part of the heat carrier, which successively transfers heat to the pyrolysis reaction mixture. As discussed earlier, the fraction enriched with solids is also placed, for example, in contact, in a reheater containing a fluidized bed of the heat carrier, with a cooling medium to reduce or limit the temperature in the reheater or, otherwise, the temperature of the recycled part of the solid heat carrier.
    Other embodiments of the invention are directed to apparatus for pyrolysis of a biomass raw material. Representative apparatuses comprise an upstream entrained bed pyrolysis reactor which may include, for example, a tubular reaction zone. The apparatus also comprises a cyclonic separator having (1) an inlet communicating with an upper section (for example, a pyrolysis effluent outlet) of the reactor, (2) a solids-enriched fraction outlet in communication with a reheater, and (3) a fractionless solids outlet in communication with a pyrolysis product condensation section. The devices further comprise a coolant distribution system in communication with the heater, for the introduction of a cooling medium and, consequently, for the removal of heat inside this container.
    Still other embodiments of the invention are directed to a reheater that serves to burn solid coal that is separated from a pyrolysis effluent. Combustion takes place in the presence of a solid heat carrier that is recycled to the pyrolysis reactor. The reheater comprises one or more points of introduction of cooling medium. In the case of multiple insertion points, these will generally be positioned at different axial lengths along the reheater. The insertion points may also include cooling medium dispensers, as well as control systems to regulate the flow of the cooling medium, for example, in response to a temperature measured either in the dense phase bed or in the diluted phase of the heat carrier. solid.
    These and other modalities and aspects related to the present invention are apparent from the Description
    Detailed below.
    BRIEF DESCRIPTION OF THE DRAWINGS
    Figure 1 describes a representative pyrolysis process that includes a reactor and a reheater.
    Figure 2 is a close-up view of a cooling medium entering a reheater both in a dense phase bed of the solid heat carrier and in a diluted phase above the dense phase bed.
    The resources referred to in Figures 1 and 2 are not necessarily drawn to scale and it should be understood that they present an illustration of the invention and / or the principles involved. Some features described have been expanded or distorted from others in order to facilitate explanation and understanding. The pyrolysis methods and apparatus, as described in this document, will have configurations, components, and operational parameters determined, in part, by the intended application and also by the environment in which they will be used.
    DETAILED DESCRIPTION
    According to representative modalities of the invention, the biomass subjected to pyrolysis in an oxygen-free environment, for example, using a Rapid Thermal Processing (RTP), can be any plant material, or mixtures of plant materials, including a wood of hardwood (for example, white wood), a softwood, or a hardwood or softwood bark. Energy crops, or otherwise agricultural waste (for example, logging waste) or other types of vegetable waste or vegetable-derived waste, can also be used as plant material. Specific exemplary plant materials include corn fiber, corn straw, and sugar cane bagasse, as well as intentional energy crops, such as switchgrass (Panicum virgatum), miscantum, and algae. Products from short-rotation crops, such as energy crops, include oak, ash, Nothofagus (southern beech), birch, eucalyptus, poplar, willow, Broussonetia papyrifera (paper mulberry), Australian acacia, plane tree, and Paulownia elongata varieties. Other examples of suitable biomass include organic waste materials, such as used paper and construction, demolition, and municipal waste.
    A representative pyrolysis method is illustrated in Figure 1. According to this embodiment, biomass 10 is combined with a solid heat carrier 12, which has been heated in a reheater 100 and recycled. Biomass 10 is generally subjected to one or more pretreatment steps (not shown), including particle size adjustment and drying, before being combined with the solid heat carrier 12. The representative average particle sizes for biomass 10 are typically from 1 mm to 10 mm. By combining with the solid heat carrier 12, biomass 10 quickly becomes heated, for example, in a mixing zone 14 located at or near a lower section (for example, the bottom) of the pyrolysis reactor 200 containing an elongated reaction zone (eg tubular) 16. The relative amount of solid heat carrier 12 can be adjusted as needed to achieve a desired rate of biomass temperature rise 10. For example, weight ratios between the carrier solid 12 and biomass 10 from 10: 1 to 500: 1 are typically used to achieve a temperature rise of 1000 ° C / sec (1800 ° F / sec) or more.
    Therefore, the combination of biomass 10 with the solid heat carrier 12 forms a hot pyrolysis reaction mixture, having a temperature generally of 300 ° C (572 ° F) to 1,100 ° C (2,012 ° F), and generally 400 ° C (752 ° F) to 700 ° C (1,292 ° F). The temperature of the pyrolysis reaction mixture is kept above its relatively short duration in the reaction zone 16, before the pyrolysis effluent 24 is separated. A typical pyrolysis reactor operates with the flow of the pyrolysis reaction mixture in an upward direction (for example, in an upstream bed pyrolysis reactor), through reaction zone 16, so that the pyrolysis conditions are met. maintained in this zone for the conversion of biomass 10. Upward flow is achieved using a carrier gas 13 containing little or no oxygen, for example, containing part or all of the non-condensable gases 18 obtained after condensing the product (s) liquid pyrolysis 20 from a fraction devoid of solids 22, which comprises a mixture of gaseous and liquid pyrolysis products. These non-condensable gases 18 normally contain H 2 , CO, CO 2 , methane, and / or ethane. Some oxygen can enter the pyrolysis reaction mixture, however, from the reheater 100, where the coal is burned in the presence of a combustion medium containing oxygen 28, as discussed in more detail below.
    The transport gas 13 is therefore charged to the pyrolysis reactor 200 at a flow rate sufficient to achieve a surface velocity of the gas through the mixing zone 14 and the reaction zone 16 which enters the majority, and generally substantially all, solid components of the pyrolysis reaction mixture. Representative surface gas velocities are greater than 1 meter per second, and generally greater than 2 meters per second. The transport gas 13 is shown in Figure 1 entering a lower section of the mixing zone 14 of the reactor 200. The surface velocity of this gas in the reaction zone 16 is also sufficient to obtain a short residence time of the pyrolysis reaction mixture in this zone, typically less than 2 seconds. As discussed earlier, rapid heating and a short duration at the reaction temperature prevent the formation of less desirable equilibrium products than less desirable non-equilibrium products. Solid heat carriers, suitable for transferring substantial amounts of heat for rapid heating of biomass 10 include inorganic particulate materials having an average particle size typically 25 microns to 1 mm. Therefore, representative solid heat carriers are inorganic refractory metal oxides, such as alumina, silica, and mixtures thereof. Sand is a preferred solid heat carrier.
    The pyrolysis reaction mixture is subjected to pyrolysis conditions, including a temperature, and a residence time over which the temperature is maintained, as discussed earlier. The pyrolysis effluent 24 comprising the solid pyrolysis by-product coal, and the solid heat carrier, and the pyrolysis products, is removed from an upper section of the pyrolysis reactor 200, such as the top of reaction zone 16 ( for example, a tubular reaction zone) of this reactor 200. The pyrolysis products, which comprise both non-condensable and condensable components of the pyrolysis effluent 24, can be recovered after separation of the solids, including coal and the heat carrier. Cooling, to promote condensation, and possibly additional separation steps are used to provide one or more liquid pyrolysis products. A particular liquid pyrolysis product of interest is crude pyrolysis oil, which generally contains 30 to 35% by weight of oxygen in the form of organic oxygenates, such as hydroxy aldehydes, hydroxy ketones, sugars, caboxylic acids, and phenolic polymers , as well as dissolved water. For this reason, although it is a pourable and transportable liquid fuel, crude pyrolysis oil has only 55-60% of the energy content of petroleum-based fuel oils. Representative values of the energy content are in the range of 19.0 MJ / liter (69,800 BTU / gal) to 25,0 MJ / liter (91,800 BTU / gal). Furthermore, this crude product is generally corrosive and exhibits chemical instability due to the presence of highly unsaturated compounds, such as olefins (including diolefins) and aromatic alkenyl.
    Therefore, the hydroprocessing of this pyrolysis oil is beneficial in terms of reducing its oxygen content and increasing its stability, thus making the hydroprocessed product more suitable for blending in fuels, such as gasoline, satisfying all applicable specifications. Hydroprocessing involves putting the pyrolysis oil in contact with hydrogen and in the presence of a suitable catalyst, generally under conditions sufficient to convert a large proportion of the organic oxygen in the crude pyrolysis oil into CO, CO 2 and water that are easily removed. The term pyrolysis oil, as it applies to a raw material in the hydroprocessing stage, refers to crude pyrolysis oil obtained directly from pyrolysis (for example, RTP) or, otherwise, it refers to this new pyrolysis oil being subjected to a pre-treatment, such as filtration to remove solids and / or ion exchange to remove soluble metals, prior to the hydroprocessing step.
    As illustrated in the modality of Figure 1, the pyrolysis effluent 24, which exits through the upper section of the pyrolysis reactor 200, is separated using a cyclone 300 in fractions enriched with solids and fractions devoid of solids 26, 22. These fractions are enriched and deprived, respectively, in their solids content, for example, measured in percentage by weight, in relation to the pyrolysis effluent 24. The fraction enriched with solids 26 comprises a substantial proportion (for example, greater than 90%, by weight ) of the solid coal and solid heat carrier contained in the pyrolysis effluent 24. In addition to coal, the fraction enriched with solids generically also contains other lower value pyrolysis by-products, such as coke and heavy tar. According to alternative modalities, multiple solids separation stages (for example, which uses two or more cyclones) can be used to improve the separation efficiency, thus generating multiple fractions enriched with solids, part or all of which enter in the reheater 100. In any case, the portion of the solid heat carrier contained in the pyrolysis effluent and which enters the reheater 100, whether in one or more fractions enriched with solids, consists of a recycled portion. This recycled portion, in addition to the solid coal leaving cyclone 300 and possibly other solid separators, enters the reheater 100 used to burn the coal and reheat the solid heat carrier for an additional use in transferring heat to biomass 10.
    The fraction devoid of solids 22 can be cooled, for example, using a cooler 400 to condense the liquid pyrolysis products as a crude pyrolysis oil and, optionally, after the additional separation / purification steps, valuable chemicals including acids carboxyls, phenolics, and ketones. As shown in Figure 1, the cooled pyrolysis product 42 is passed to separator 500 which can be a single stage instant separator to separate non-condensable gases 18 from liquid pyrolysis products 20. Otherwise, multiple vapor equilibrium stages and liquid in contact can be obtained using suitable contact devices, such as contact trays or solid packaging materials.
    In general, it is desired that the rapid cooling of the fraction devoid of solids 22 limits the extent of pyrolysis reactions that occur beyond the relatively short residence time in reaction zone 16. Cooling can be achieved using direct heat exchange or indirect, or both types of heat exchange in combination. An example of types of heat exchange involves the use of a cooling tower in which a condensed liquid pyrolysis product is cooled indirectly, recycled at the top of the tower, and placed in countercurrent with the hot steam in elevation of the fraction devoid of solids 22. As previously discussed, the fraction devoid of solids 22 comprises gaseous and liquid pyrolysis products, including crude pyrolysis oil which is recovered in downstream processing. Correspondingly, cyclone 300 has (i) an input in communication with an upper section of the pyrolysis reactor 200, in addition to (ii) a fraction output enriched with solids in communication with the reheater 100 and (iii) an output of fraction devoid of solids in communication with a condensation section of pyrolysis product. That is, the cyclone inlet can correspond to the conduit for the pyrolysis effluent 24, the solids-enriched fraction outlet can correspond to the solids-enriched fraction conduit, and the non-solids fraction outlet can correspond to the conduit for the solids. fraction devoid of solids 22. A representative pyrolysis product condensation section may correspond to cooler 400 and separator 500.
    As illustrated in the representative embodiment of Figure 1, the fraction enriched with solids 26 leaving cyclone 300 (possibly in combination with one or more fractions enriched with additional solids) is brought into contact with a combustion medium containing oxygen 28 in the reheater 100 to burn at least a portion of the solid coal that enters this container with the fraction enriched with solids 26. A representative oxygen-containing combustion medium is air. Nitrogen-enriched air can be used to limit the rise in adiabatic combustion temperature, if desired. The heat of combustion effectively reheats the recycled portion of the solid conveyor. In turn, the heated solid carrier is used for continuous heat transfer to the pyrolysis reaction mixture in order to conduct the pyrolysis reaction. As previously discussed, the heater 100 generally operates as a fluidized bed of solid particles, with the combustion medium containing oxygen serving as a fluidizing medium, similarly in operation to a catalyst regenerator in a fluid catalytic cracking process ( FCC), used in the refinement of crude oil. Combustion generates flue gas 32 exiting reheater 100, and, according to some embodiments, flue gas 32 can be passed to a solids separator, such as cyclone 300 to remove entrained solids. The fluidized bed comprises a dense phase bed 30 (e.g., a bubble-free, bubbling, evaporative, turbulent, or fast fluidized bed) of the solid heat carrier in a lower section of the heater 100, below a diluted phase 40 of these particles , in an upper section of the reheater 100. One or more cyclones can also be internal to the reheater 100, to achieve the desired separation of entrained solid particles and return to the dense phase bed 30.
    Aspects of the invention refer to the use of a cooling medium to improve the general management of heat in pyrolysis systems. For example, the removal of heat from the solid carrier, and the transfer of heat to the cooling medium, can be achieved by a direct exchange of heat between the cooling medium and the solid carrier. Advantageously, the temperature of the recycled portion of the solid heat carrier, which is passed to the heater 100 as described above, is limited (for example, to a maximum design temperature) by direct contact between this solid heat carrier and the cooling medium. cooling 44 in reheater 100. In some cases, this limitation of the combustion temperature may allow an increase in the operational capacity of the general pyrolysis system. A preferred cooling medium is water or an aqueous solution having a pH that may be suitable for the building material of the heater or, otherwise, may have the ability to neutralize flue gases at elevation. In some cases, for example, the use of a diluted caustic solution, having a pH in the range of 8 to 12, can effectively neutralize the acidic components present in the flue gases. Preferably, the cooling medium 44 is introduced to the heater 100 through the distributor 46.
    Figure 2 illustrates, in greater detail, a particular way of putting the cooling medium in contact with the fraction enriched with solids recovered from the pyrolysis effluent. According to this modality, a coolant distribution and control system is in communication with the reheater. In particular, Figure 2 shows the portions of a cooling medium 44a, 44b being introduced into the heater 100 at two separate points (to which the ducts for the cooling medium portions 44a, 44b lead) along their axial length. In general, therefore, the cooling medium can be introduced in one or more positions along the axial length of the heater and / or in one or more radial positions at a given axial length. Likewise, the cooling medium can be introduced through one or more dispensers in one or more introduction positions. According to the embodiment described in Figure 2, a portion of the cooling medium 44b is introduced into the heater 100 above the dense phase bed 30 of the solid particulate which comprises a recycled portion of the solid heat carrier, as described above. This portion of the cooling medium is directed downwardly to the surface of the dense phase bed 30, however, a break in the bed is relatively minor, since the vaporization of the cooling medium occurs primarily in the diluted phase 40. In Figure 2, , also, another portion of the cooling medium 44a, introduced into the dense phase bed 30 of the solid heat carrier, through the distributor 46. The interruption of the dense phase bed 30 is increased, however, a direct heat transfer is also increased in relation to the case of introducing the cooling medium portion 44b into the diluted phase 40. The introduction of the cooling medium both in the dense phase bed 30 and in the diluted phase 40, for example, at different rates and / or at different times therefore, it allows alternative types of control (for example, coarse control and fine control, respectively) of heat removal. In accordance with additional embodiments, the methods described in this document may further comprise, at least a portion of the solid heat carrier flowing through a heat exchanger (not shown), such as a sand cooler, thus adding another type of removal control.
    In accordance with the coolant distribution and control system described in the particular embodiment of Figure 2, the flows of portions of the cooling medium 44a, 44b, introduced into and above the dense phase bed 30, are controlled in response to temperatures measured inside and above the dense phase bed 30, respectively. Therefore, the temperature elements TE in the dense phase bed 30 and in the diluted phase 40, communicate via TT temperature transmitters and TIC temperature indicating controllers to the TV temperature control valves. These valves, in response to the measured temperatures, adjust their variable percentage openings as needed to provide sufficient flows of portions of the cooling medium 44a, 44b in order to control the temperatures measured at temperature elements E. Therefore, in response to a temperature measured in reheater 100 which is beyond a setpoint temperature, for example, due to an increase in flow rate, or a change in type, of biomass 10, the appropriate ICT (s) sends signal (s) to the corresponding temperature control valve (s), which responds by increasing the flow rate of the cooling medium to the reheater 100, optionally via one or more distributors 46. Correspondingly, the coolant distribution and control systems described in this document can effectively provide the greatest operational flexibility required in pyrolysis operations, where and whether increased capacity and / or processing of variable biomass types is desired. Therefore, the particular coolant distribution and control systems are represented by the combination of TE, TT, TIC, and TV, controlling the introduction of the cooling medium at a given point.
    In general, aspects of the invention focus on pyrolysis methods with improved heat control, and especially reheaters for burning solid coal, separated from a pyrolysis effluent, in the presence of a solid heat carrier that is recycled to the reactor. pyrolysis to transfer heat and lead to pyrolysis. Advantageously, the reheater comprises one or more points of introduction of cooling medium along its axial length, optionally next to the distribution and control systems of cooling medium, as previously described. Individuals skilled in the art, with the knowledge gained from the present disclosure, will recognize that various changes could be made to these methods and pyrolysis without departing from the scope of the present invention. The mechanisms used to explain the 5 theoretical or observed phenomena or results, should be interpreted only as illustrative and not in any way limiting the scope of the attached claims.
    权利要求:
    Claims (6)
    [1]
    1. Pyrolysis method, characterized by the fact that it comprises:
    (a) combining a biomass and a solid heat carrier to provide a pyrolysis reaction mixture;
    (B) to submit the mixture reaction in pyrolysis The conditions pyrolysis for provide one effluent in pyrolysis;(ç) to separate, from the effluent from pyrolysis, (1) an
    fraction enriched with solids comprising solid coal and a recycled portion of the solid heat carrier and (2) a fraction devoid of solids comprising products of gaseous and liquid pyrolysis;
    (d) placing in a reheater the fraction enriched with solids in direct contact with (1) a combustion medium containing oxygen to burn at least a portion of the solid coal and reheat the recycled portion of the solid heat carrier and (2) a medium cooling to limit the temperature of the recycled portion of the solid heat carrier, where at least a portion of the cooling medium is introduced into the reheater in a liquid state within a dense phase bed of the heat carrier.
    [2]
    2/2 characterized by the fact that the cooling medium is introduced to the reheater through one or more distributors in one or more positions in which the cooling medium is introduced.
    2. Method according to claim 1, characterized by the fact that the cooling medium is introduced to the reheater in one or more positions along its axial length.
    [3]
    3. Method according to claim 1,
    Petition 870190028165, of 03/25/2019, p. 7/23
    [4]
    Method according to claim 1, characterized in that the at least a portion of the cooling medium is a portion of the cooling medium, and an additional portion of the cooling medium is introduced to the heater above the phase bed dense heat carrier.
    [5]
    5. Method according to claim 4, characterized in that the flow of the additional portion of the cooling medium introduced to the heater above the dense phase bed is controlled in response to a measured temperature above the dense phase bed.
    [6]
    6. Method, in wake up with The claim 4, characterized by fact that the additional portion of the medium in cooling is directed downwards to the surface of dense phase bed . 7. Method, in wake up with The claim 1, characterized by fact that the middle cooling comprises water.8. Method, in wake up with The claim 1, characterized by fact that the flow at least an
    A portion of the cooling medium introduced into the reheater in a liquid state within the dense phase bed is controlled in response to a temperature measured within the dense phase bed.
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    US20120214113A1|2012-08-23|
    RU2013143017A|2015-04-10|
    CN103649276A|2014-03-19|
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    WO2012115754A2|2012-08-30|
    MY178211A|2020-10-07|
    CA2828037C|2019-03-12|
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    BR112013021459A2|2016-10-25|
    DK2678405T3|2018-08-27|
    CN103649276B|2015-11-25|
    EP2678405B1|2018-07-25|
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    法律状态:
    2019-01-02| B07A| Application suspended after technical examination (opinion) [chapter 7.1 patent gazette]|
    2019-08-13| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2019-10-01| 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 01/02/2012, OBSERVADAS AS CONDICOES LEGAIS. (CO) 20 (VINTE) ANOS CONTADOS A PARTIR DE 01/02/2012, OBSERVADAS AS CONDICOES LEGAIS |
    优先权:
    申请号 | 申请日 | 专利标题
    US13/031,701|2011-02-22|
    US13/031,701|US9441887B2|2011-02-22|2011-02-22|Heat removal and recovery in biomass pyrolysis|
    PCT/US2012/023460|WO2012115754A2|2011-02-22|2012-02-01|Heat removal and recovery in biomass pyrolysis|
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