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    • 专利摘要:
    Various aspects provide for a multistage fluidized bed reactor (300, 400, 500, 600), particularly comprising a volatilization stage (310) and a combustion stage (330). The gas phases above the bed solids in the respective stages are separated by a wall (320). An opening (e.g., in the wall) provides for transport of the bed solids from the volatilization stage (310) to the combustion stage (310). Active control of the gas pressure in the two stages may be used to control bed solids flow. Various aspects provide for a fuel stream processing system (200) having a pretreatment reactor (210), a combustion reactor (230), and optionally a condensation reactor. The condensation reactor receives a volatiles stream volatilized by the volatilization reactor. The combustion reactor receives a char stream resulting from the removal of the volatiles by the volatilization reactor.
    公开号:FI20170148A1
    申请号:FI20170148
    申请日:2017-11-01
    公开日:2018-12-10
    发明作者:Henrik Ström；David Pallarés；Henrik Thunman；Martin Seemann；Christer Gustavsson
    申请人:Bioshare Ab；
    IPC主号:
    专利说明:

    BACKGROUND
    1. Technical Field [0001] The present invention relates generally to the recovery of volatile species from fuels, and more particularly to the extraction and/or isolation of chemicals from fuel streams in fluidized bed systems.
    2. Description of Related Art [0002] A combustion plant bums a fuel (e.g., wood, coal, gas, oil, waste products, and the like) to generate useful heat and/or electricity. A Combined Heat and Power (CHP) plant may generate electricity using a first portion of the combustion heat to drive a turbine and then a remaining portion of heat in another process (e.g,, in a second thermal cycle, for industrial use, for district heating, and the like).
    [0003] FIG. 1 illustrates a typical fluidized bed (FB) boiler 100, in which a granular bed of bed solids (e.g., sand) suspends the (typically solid pieces of) fuel within a combustion container. Air flows upward through holes in a distributor plate in the floor of the combustion container. Using appropriately sized solid particles, air distribution plate, and air flow, the bed becomes fluidized by the upwardly flowing air. A fluidized bed may behave as a liquid, notwithstanding that the bed is formed primarily of solid particles intermingled with a gas phase. In a typical fluidized bed plant, the fuel is ground or cut into pieces, which are fed into the fluidized bed to combust with incoming air (e.g., from the bottom of the bed, also possibly from the side) to generate heat. Combustion heat is often used to generate steam, which may be used directly and/or converted to electricity. The resulting flue gas is treated to remove dust (e.g., as fly ash, bottom ash) and then exhausted to the atmosphere.
    [0004]
    P0017FI
    SUMMARY [0005] Various aspects provide for a multistage fluidized bed reactor comprising separate stages (typically separated by one or more walls). Independent control of the gas pressure between the stages, combined with an appropriately dimensioned communication passage between the stages, enables a controlled transport of media (gas, bed solids) between the beds. Various aspects may be used to control residence times and reaction rates within a stage, and heat and/or mass transfer between the stages, enabling a wide range of chemical reactions.
    [0006] In an embodiment, a fluidized bed reactor configured to react a fuel in a fluidized bed of bed solids comprises one or more containers configured to hold the bed of solids, and one or more walls separating the container(s) into at least a volatilization stage and a combustion stage. Typically, a single container includes both the volatilization and combustion stages sharing a common bed, with a wall separating the gas phases of the stages, and each stage having its own gas supply for fluidization.
    [0007] The wall between the volatilization and combustion stages separates at least the gas phases in the stages. An opening between the stages provides for transport of bed solids and char between the stages. The opening may be in the wall separating the stages. The opening may be in the floors of the stages (e.g., openings in the floors connected via a pipe).
    [0008] The volatilization stage has a fuel inlet configured to receive the fuel, and one or more inert gas inlets at the bottom of the container. An inert gas supply configured to supply (typically hot) volatilization gas to the inert gas inlets provides a gas pressure and flow rate sufficient to fluidize the bed solids and volatilize the fuel to yield a (predominantly gaseous) volatiles stream and a char stream (comprising residual carbonaceous species, or char). Typically, an inert, reducing, or mildly oxidizing gas (e.g., Νϊ, syngas, steam, and the like) is used in the volatilization stage. A volatiles stream outlet conveys the volatiles stream out of the volatilization stage and a char stream outlet may convey the char stream (and typically some bed solids) out of the volatilization stage via the opening. A volatiles stream is typically predominantly gaseous, possibly with some small entrained particulates of liquid or solid (e.g., mist, dust). In an embodiment, the volatiles stream comprises biomass vapor, raw gas, wood gas, droplets of biomass, and the like.
    P0017FI [0009] The combustion stage may have a char stream inlet configured to receive the char stream (typically with some bed solids) from the volatilization stage. One or more oxidant gas (eg., air) inlets at the bottom of the combustion stage are coupled to an oxidizing gas supply configured to fluidize the bed of solids in the combustion stage and combust the char stream to yield an exhaust gas. Typically, an air supply supplies air to the oxidant inlets at the bottom of the combustion stage. An exhaust gas outlet conveys the exhaust gas out of the combustion stage. Typically, the exhaust gas is used to generate electricity (eg., with a gas turbine and/or steam turbine), and or may flow through a heat exchanger for extraction of the exhaust heat (e.g., for district heating, process heat, and the like).
    [0010] An opening (e.g., in the wall or floor) couples the fluidized beds in the volatilization and combustion stages (eg., via the char stream outlet/inlet) such that bed solids and char may flow between the stages, even though the gas phases are substantially separated. The volatilization stage includes a volatiles pressure gauge configured to measure the gas pressure within the volatilization stage, and the combustion stage includes a combustion pressure gauge configured to measure pressure within the combustion stage.
    [0011] The reactor includes one or more means to control gas flow into and/or out of a stage. The combustion stage may include a volatiles outlet valve fluidically coupled to the volatiles stream outlet (typically sufficiently downstream to prevent fouling and/or problems due to high temperature) and configured to controllably restrict gas flow through the volatiles stream outlet. The combustion stage may include an exhaust valve (e.g., coupled to the exhaust gas outlet) configured to controllably restrict gas flow out of the combustion stage. Either or both stages may include a fan (e.g., coupled to a fuel inlet or gas outlet, such as an induced draft fan) configured to controllably pump gas into or extract gas from the stage. A controllable gas source may be used to pressurize a stage. Pressure of the fluidizing gas (eg., the inert gas supply and/or the oxidant supply) may be used to control pressure within a stage.
    [0012] A controller is coupled to the pressure gauges and configured to measure the pressures within the volatilization and combustion stages (e.g., to measure a pressure difference). The controller is coupled to means to control gas flow, such that a desired pressure difference between stages (according to the pressure gauges) may be maintained via operation of the gas flow means, typically using closed-loop control. Typically, a
    P0017FI controller might control a volatiles outlet valve (restricting gas flow out of the volatilization stage) and/or an exhaust fan (extracting gas from the combustion stage).
    [0013] The controller operates the gas flow control means to achieve a desired pressure difference between the beds, which may be used to control residence time, reaction rates, convection (within and between beds), and/or the transfer rate of char from the volatilization stage to the combustion stage. During steady state operation, the controller may control the residence time of fuel particles via the pressure difference. A longer residence might lead to an increased degree of volatilization (and thereby to a reduced amount (flow) of char). Typically, the controller controls the pressure in the volatilization stage to be greater than the pressure in the combustion stage. This pressure difference may be used to controllably drive a flow of the char stream and bed solids from the volatilization stage to the combustion stage via the opening/char stream outlet/char stream inlet.
    [0014] The separation of the gas phases in the volatilization and combustion stages enables the use of different fluidization gases in the respective stages and/or the production of different chemical species within each stage. An inert and/or reducing gas is typically used for fluidization in the volatilization stage. The volatilization stage volatilizes (e.g., pyrolyzes/gasifies/evaporates/reforms) or otherwise reacts the fuel to form volatiles and char, after which the char is transferred to the combustion stage. Volatilization may include partial oxidation, but typically does not result in complete oxidation (thus the residual char). An oxidizing gas (e.g., air) is typically used in the combustion stage.
    [0015] The system may include a separation reactor configured to receive the volatiles stream from the volatilization stage. The separation reactor may include a heat exchanger, a condenser, a separator configured to separate phases, species, and the like, a cyclone, and the like.
    [0016] The system may include a heat exchanger coupled to the exhaust gas outlet and the inert gas supply and configured to transfer heat from the combustion stage to pre-heat the inert gas used in the volatilization stage. A heat exchanger may improve the thermal efficiency of the system. A heat exchanger may be coupled to a volatiles stream (e.g., to condense species out of the stream).
    [0017] A stage may comprise one or more internal walls and/or baffles. A volatilization stage may include an internal wall between the fuel inlet and volatiles stream
    P0017FI outlet, configured to separate the gas phase proximate to the fuel inlet from the volatiles exiting the volatilization stage. Typically, the internal wall extends down into the fluidized bed. In some cases the wall ends just above the fluidized bed (allowing some gas phase transfer). In some cases the wall extends into the fluidized bed (preventing gas transfer). Such a configuration may obligate incoming fuel and/or volatile species to pass through the bed for at least some time. In an embodiment, an internal wall separates the volatilization stage into an inlet stage and a reforming stage.
    [0018] A stage separated by a wall may include separate pressure gauges and valves, correspondingly coupled to the controller to provide for independent pressure control over the various portions of the stage. For example, an internal wall may extend into the bed in the volatilization stage, separating the volatiEzation stage into an inlet stage (with the fuel inlet) having an inlet pressure gauge (and optionally an inlet gas valve and/or inlet gas supply) and a reforming stage having a reforming pressure gauge and the volatiles stream outlet. The controller may be coupled to the gauges and/or valves and further configured to independently control the gas pressures of the inlet stage, reforming stage, and/or combustion stages.
    [0019] A stage may comprise a baffle disposed at the bottom of the bed, at the top of the bed (e.g., from below the bed surface to above the bed surface) and/or within the bed. A baffle disposed at the top of the bed may block solid material (e.g., floating on top of the bed solids) while allowing mass transfer below or above the baffle. In an embodiment, the volatilization stage (e.g., an inlet stage) includes a baffle disposed at the top of the bed, configured to force non-gaseous phases within the bed (e.g., fuel, char, or other condensed phases) to pass below the baffle (e.g., to get from the inlet stage to the volatilization stage or the combustion stage). A baffle may be used to impart a minimum residence time within the bed, which may more fully react large pieces of fuel.
    [0020] Various aspects provide for a fuel stream processing system to pre-treat a fuel stream to extract volatile species from the fuel prior to combustion, rather than burning them immediately. A pretreatment reactor may pretreatthe fuel stream via heating in an inert, partially oxidizing, and/or reducing environment to volatilize/pyrolyze/gasify/reform various molecules. A pretreatment reactor outputs a
    P0017FI volatiles stream that (according to fuel and reaction conditions) may include syngas, gaseous species, biofuels and/or biofuel precursors, chemicals, and the like.
    [0021] The pretreatment reactor may include a volatilization stage, and in some cases, a fast flash pyrolysis reactor is used. In the case of flash pyrolysis, the volatiles stream is conveyed from the pyrolysis reactor to a separation/condensation/fractionation reactor, which quickly condenses the volatiles and segregates them (e.g., by condensation point). Pretreatment may (but need not) be performed in a fluidized bed reactor, which may be fluidically coupled to a combustion reactor (e.g., a fluidized bed combustor) via the bed solids. A cyclone may be implemented to separate various species. The segregated species may be removed for subsequent use (e.g., purification, additional processing). A residual stream may be sent from the condensation/fractionation reactor to the FB combustor for burning.
    [0022] A multistage fluidized bed reactor (e.g., comprising separate volatilization and combustion stages) may be implemented as a fuel stream processing system. For convenience, certain components (e.g., inlets, outlets) of such a reactor are illustrated in the context of a fuel stream processing system.
    [0023] A method may comprise delivering a fuel (e.g., wood, straw, garbage, MSW, sewage, and the like) to the volatilization stage, fluidizing the fluidized bed in the volatilization stage with the inert and/or reducing gas, and volatilizing at least a portion of the fuel. A method may comprise controlling a flow of char and bed solids from the volatilization stage to the combustion stage by controlling a pressure difference between the stages. Residence times and/or convection within and/or between stages may be used to control reaction rates, heat transfer, and mass transfer within and/or between stages.
    BRIEF DESCRIPTION OF THE FIGURES [0024] FIG. 1 is a schematic illustration of a typical fluidized bed boiler.
    [0025] FIG. 2 is a schematic illustration of a fuel stream processing system, per some embodiments.
    [0026] FIG. 3 is a schematic illustration of a two-stage fluidized bed reactor, per some embodiments.
    P0017FI [0027] FIG. 4 is a schematic illustration of a two-stage fluidized bed reactor, per some embodiments.
    [0028] FIG. 5 illustrates a three-stage reactor with an internal wall separating the gas phases of the fuel inlet and volatiles outlet, per some embodiments.
    [0029] FIG. 6 illustrates a three-stage reactor with an internal wall separating the gas phases of the fuel inlet and volatiles outlet, per some embodiments.
    DETAILED DESCRIPTION [0030] The reduction, reuse, and recycling of waste streams is an increasingly important priority in many societies. Some waste streams are burned (e.g., for heat and/or electricity). While combustion might utilize the fuel value of a waste stream, the chemical properties of certain components of the fuel might be substantially more valuable if they were they utilized for chemical purposes, rather than as fuel. Some waste streams (municipal solid waste, dehydrated sewage) contain small quantities of chemicals that have very high value. Certain components of biomass (e.g., wood species) may have very high value. The present description incorporates by reference US provisional patent application no. 62/517,186, filed June 9,2017.
    [0031] Both waste fuel streams and nonwasted fuel streams, such as petrochemicals, biomass and the like, municipal solid waste (MSW), sewage, and the like, comprise a wide range of molecules. Some of these molecules (or portions thereof) are valuable beyond their use as a fuel supply. Systems and methods described herein may be implemented to recover chemicals that might otherwise be combusted, enabling the subsequent use of these chemicals in higher-value applications.
    [0032] A fuel stream processing system may comprise a pretreatment reactor (e.g., to pyrolyze/evaporate/volatilize/gasify/reform a fuel) and a combustion plant. A fuel stream flows into the pretreatment reactor to be reacted to form a volatiles stream and a char stream. The pretreatment reactor may pyrolyze/gasify/volatilize/precombust or otherwise react a solid or liquid fuel prior to its passage to the combustion plant, typically with an inert, reducing, or mildly oxidizing gas (e.g., N2, syngas, steam, and the like). The char stream flows into the combustion plant, where it is combusted. The pretreatment reactor may be retrofit to an existing combustion plant (e.g., with an additional fuel supply).
    P0017FI [0033] A volatiles stream may be used directly. For example, a fuel may be separated into a first fuel source (e.g., for a separate combustion process, such as an engine or turbine) and a residual char source (e.g., for combustion in a fluidized bed). A volatiles stream may flow to a separation reactor, which typically cools the volatiles stream to condense and separate out one or more (typically >5, including >10, including >100) chemical species from the volatiles stream. The separated chemical species may be subsequently processed and/or utilized. The chemical species may include syngas (H2 + CO), gaseous hydrocarbons (including oxygenated hydrocarbons), liquid fuels (e.g., C4-C16) such as biofuels and/or biofuel precursors, volatile polymers, fuel gas, chemical compounds, fine chemicals, and the like. A residual stream (remaining, undesired chemicals which may have fuel value) may be routed to the combustion plant and combusted.
    [0034] FIG. 2 is a schematic illustration of a fuel stream processing system, per some embodiments. A fuel stream processing system 200 may comprise a pretreatment reactor 210 fluidically coupled to a combustion reactor 230. The pretreatment reactor volatilizes an incoming fuel stream to form a volatiles stream. Nonvolatilized fuel (char) is typically conveyed from the pretreatment reactor to a combustion reactor via a char stream, which bums the char stream to extract the heat value. The system may include a separation reactor 220 coupled to one or both of the reactors 210,230. The pretreatment reactor may be retrofit to an existing combustion reactor (each reactor may have its own fuel supply).
    [0035] Pretreatment reactor 210 receives the fuel stream via a fuel inlet 216, and pretreats (e.g., volatilizes/gasifies/pyrolyzes/reforms/reacts) a portion of the received fuel to yield a volatiles stream and a char stream. Pretreatment/volatilization typically comprises treating the fuel in a reaction zone 212 with an inert or reducing gas, delivered via gas inlet 214 from a gas supply 211. The pretreatment reactor outputs a volatiles stream via a volatiles stream outlet 218. The char stream is output via a char stream outlet 219 to a char stream inlet 239 of the combustion reactor 230. The pretreatment reactor and combustion reactor may be discrete (e.g., with the char stream outlet/inlet coupled via a passage 299). The pretreatment reactor and combustion reactor may be integrated (e.g., with the char stream outlet/inlet forming an opening in a wall between the reactors). In some cases, to prevent undesired reactions (e.g., polymerization, decomposition, precipitation), the
    P0017FI pretreatment reactor may include a fast pyrolysis reactor (e.g., that constrains volatiles to a residence time below 10 seconds, including below 3 seconds).
    [0036] Combustion reactor 230 (e.g., a combined heat and power plant) includes a combustion zone 232 within which the char stream is reacted with an oxidant gas (e.g., air, oxygen, and the like). An oxidant supply 231 delivers oxidant via an oxidant inlet 234. In some embodiments, one or both of the inlets 214,234 comprise diffuser plates (e.g., such that the respective reactors can function as fluidized beds). Combustion reactor 230 includes an exhaust 237, and may include an optional second fuel inlet 236 configured to deliver a fuel directly into the combustion reactor. Combustion of char may be augmented with fuel from the second fuel inlet 236 and corresponding supplementary fuel supply (not shown), which may be the main fuel supply to the combustion reactor.
    [0037] The volatiles stream outlet of the pretreatment reactor may be coupled to a separation reactor 220 (e.g., a fast condensation/fractionation reactor, a cyclone, and the like) via a volatiles stream inlet 222. Separation reactor 220 may extract and/or isolate desirable chemicals from the volatiles stream. A heat exchanger 224 (e.g., coupled to the separation reactor) may be used to remove heat from the volatiles stream, enhancing condensation. A separation reactor may include a phase separator 226 configured to separate condensed species from more volatile species (e.g., a cyclone). In some cases, separation reactor 220 outputs a residuals stream (e.g., comprising residual chemicals not extracted for other purposes) via residuals stream outlet 228. Residuals stream outlet 228 may be coupled to a corresponding residuals stream inlet 238 of the combustion reactor, providing for the combustion of the residuals stream. A heat exchanger 240 may be coupled to the exhaust stream (e.g., via exhaust 237) of the combustion reactor 230 to preheat the inert/reducing gas prior to its introduction into the pretreatment reactor via gas inlet 214.
    [0038] A volatiles stream may have a range of uses (according to fuel source, pretreatment conditions, and the like) such as for raw gas, syngas, and the like. The volatiles stream may include syngas (e.g., for use in a subsequent chemical process) gaseous species (e.g., gaseous fuels), liquid fuels (e.g., biofuels and/or biofuel precursors), and the like.
    [0039] A fuel stream processing system may comprise one or more fluidized bed reactors. For example, pretreatment reactor 210 may be configured as a volatilization stage
    P0017FI of a fluidized bed reactor as described herein, and combustion reactor 230 may be configured as a combustion stage of a fluidized bed reactor as described herein. The reactors may share a fluidized bed of solids (e.g., separated by a wall) providing for a flow of char (and typically bed solids) from the pretreatment reactor to the combustion reactor. The system may be implemented as a standalone system and/or retrofit to an existing combustion reactor (e.g., an existing fluidized bed boiler). The fuel stream processing system need not incorporate a fluidized bed reactor.
    [0040] FIG. 3 is a schematic illustration of a two-stage fluidized bed reactor, per some embodiments. A multistage fluidized bed reactor comprises a fluidized bed having at least a first (e.g., volatilization) and second (e.g., combustion) stages, each stage enabling a different chemical reaction. In this example, a first reaction zone 312 in a first fluidized bed and a second reaction zone 332 in a second fluidized bed provide for different reactions.
    [0041] The first and second stages are separated, typically by a wall. The wall separates the gas phases above each stage, but allows the fluidized bed phases to communicate via an opening in the wall and/or a passage between beds of the stages. Thus, the fluidized bed phase (e.g., media and char stream) may pass from the first stage to the second stage, but the gas phase above the first stage is separated from the gas phase above the second stage. The fluidized beds may communicate via openings in the floor rather than the wall. The transfer of fuel and bed material from the first to second stages is typically controlled via an increased gas pressure in the first stage vs. that in the second stage. A controller coupled to pressure gauges within the stages may control these pressures (e.g., via a valve on the volatiles stream) to achieve a desired overpressure of the first stage vs. the second stage.
    [0042] In exemplary FIG. 3, a fluidized bed reactor 300 comprises a container 301 (in this example, a single container) configured to hold a bed of bed solids. A wall 302 separates the container into a volatilization stage 310 and a combustion stage 330. Wall 302 may have an opening 304 through which bed solids and char may flow. Opening 302 may include char stream outlet 219, char stream inlet 239, and/or passage 299 (FIG. 2). Opening 304 may comprise openings in the floors of each stage, coupled by a passage. Wall 302 may include a plurality of walls. The media and char stream pass from the volatilization stage to the combustion stage, where the char is burned. The wall lets the media/char pass between
    P0017FI stages, but prevents mixing of the gas phase in the volatilization stage with the oxidizing gas phase in the combustion stage.
    [0043] The volatilization stage has a fuel inlet 316 configured to receive and deliver the fuel into the volatilization stage. The fuel inlet may include a lock hopper and/or other apparatus to transfer solid fuel while controlling gas flow/pressure. Fuel may be fed by gravity and/or auger. Fuel may be delivered to the lock hopper (e.g., via a feed screw) and a gas pressure within the lock hopper may be controlled to match that of the volatilization stage, such that fuel may be delivered to the volatilization stage at or above the pressure of the volatilization stage.
    [0044] The bed solids are fluidized by a flow of gas from an inert gas supply 311 delivered via a gas inlet 314 (e.g., a diffuser plate/distributor plate having holes distributed across the plate to fluidized the bed) corresponding to the portion of the container (or the container) associated with the volatilization stage. Inert gas supply 311 supplies a (typically hot) gas chosen according to desired volatilization conditions (e.g., inert, reducing, mildly oxidizing), fuel source, desired composition of volatiles stream, and the like. Pressure drop across the distributor plate may be controlled (typically in concert with gas pressure at the top of the bed) to achieve a desired bubble size (within the bed), convection pattern, fuel residence time, bed temperature, and the like. Bed temperature may be controlled via stage pressure (e.g., to control bed height, reaction rates, and/or residence times). A typical volatilization stage may have a lower temperature at the top of the bed than at the bottom (although in the absolute bottom of the bed (the first centimeters from the bottom) where the fluidization media enters the bed the temperature is typically lower). A reduced bed height in the volatilization stage typically reduces residence time within.
    [0045] A volatiles stream outlet 318 is configured to convey the volatiles stream out of the volatilization stage (e.g., to an optional separation reactor 220). Useful species are typically extracted from the volatiles stream, and residual species from the volatiles stream may be sent to the combustion stage via a residuals line, where they are burned (FIG. 2). A volatiles pressure gauge 350 measures gas pressure in the volatilization stage, the volatiles stream outlet, and/or the corresponding volatiles line.
    [0046] A reactor includes a means to control gas flow into and/or out of at least one stage, including multiple stages. Controlling this means in concert with pressure
    P0017FI measurements, the controller may control the pressure difference between stages, typically via closed-loop (e.g., PID) control. In an embodiment, a volatiles outlet valve 370 (e.g., a butterfly valve) coupled to the volatilization stage outlet 318 is configured to control pressure in the volatilization stage and/or flow out of the volatiles stream outlet.
    [0047] Combustion stage 330 includes an oxidant inlet 334 (e.g., a diffuser plate) correspondingly disposed at the portion of the container associated with combustion. An oxidant supply 331 coupled to the oxidant inlet delivers an oxidizing gas (typically air) at a flow rate and pressure sufficient to fluidized the bed solids in the combustion stage and combust the char from the volatilization stage. An exhaust gas outlet 337 removes combustion products from the combustion stage. Heat, chemical species (e.g., ash, bed solids) and/or power may be subsequently harvested from the exhaust gas (e.g., via a heat exchanger, a turbine, and the like). A combustion pressure gauge 352 disposed in the combustion stage and/or exhaust measures pressure in the combustion stage. Reactor 300 illustrates an optional 2nd oxidant inlet 333 (e.g., to provide additional combustion air to supplement oxidant supplied via oxidant inlet 334). Additional gas and/or oxidant inlets may be included with the relevant stage. In this example, a fan 338 fluidically coupled to the exhaust 337 controllably extracts exhaust gas, which may be used to control pressure.
    [0048] A controller 360 coupled to the pressure gauges (in this case, 350, 352) controls a pressure difference between the stages. In FIG. 1, controller 360 is coupled to the volatiles outlet valve 370, and controls pressure in the volatilization stage via throttling of the valve. During operation, controller 360 typically controls pressure of the volatilization stage to exceed that of the combustion stage, driving char from the volatilization stage to the combustion stage. Pressures may be controlled via a valve on the flue gas line. Pressure control of bed solids flow (and the resulting mass transfer rates) may be used to control residence time within the stages (e.g., in a pretreatment stage prior to a combustion stage).
    [0049] A combustion stage may include a second fuel inlet 336 (e.g., to supplement the fuel value of the char), which may include a separate (or the same) fuel supply, typically with its own lock hopper. Second fuel inlet 336 may be the main fuel supply for the combustion stage, with a separate fuel supply implemented for the volatilization stage (e.g., as a retrofit to an existing combustion stage).
    P0017FI [0050] The reactor may include a heat exchanger 340 configured to extract heat from the exhaust gas and transfer the heat to the gas supplied to the volatilization stage and/or the combustion stage, which may improve energy efficiency.
    [0051] Increased gas pressure in the first stage may drive char and bed material into the second stage. In some cases, natural convection of the bed material recirculates at least some media back into the first stage from the second stage. FIG. 3 illustrates an implementation in which the floor heights of the two stages are the same; the floor heights may be different.
    [0052] The combustion stage of the fluidized bed reactor bums the char stream. In some cases, a residual stream from a separation reactor 220 is routed into the combustion stage 330, where it is burned. The hot flue gas from the second stage is used (e.g., to generate steam, heat, etc.). A portion of the hot flue gas may be routed through an optional heat exchanger 340 to preheat the inert/reducing gas flowing into the first stage. The combustion stage may have an additional fuel supply (not shown).
    [0053] FIG. 4 illustrates a two-stage fluidized bed reactor, per some embodiments. FIG. 4 schematically illustrates an exemplary effect of overpressure in the volatilization stage on the difference in the surface heights of the beds in the two stages. A volatilization stage 310 may have a fuel inlet 316 and volatiles stream outlet 318 separated by an internal wall 402. In this example, an internal wall 402 separates at least a portion of the gas phases of the fuel inlet and volatiles outlet, so that fuel passes into the bed without interfering with the volatiles exiting the volatilization stage. In FIG. 4, wall 402 does not extend into the fluidized bed of the volatilization stage 310, allowing for gaseous communication between the fuel inlet and volatiles outlet without going through the bed. The volatiles outlet and fuel inlet are held at the same pressure in this example. FIG. 4 illustrates a slanted fuel inlet 316, which may enhance gravity assist. Other gravity-assisted mechanisms may be used. Insulation or thermally conductive material may be incorporated into wall 302 to reduce or increase heat transfer through wall 302. The wall 302 separating the volatilization and combustion stages may be slanted.
    [0054] Wall 302 need not extend into the bed solids at the same location as the transition between the gas inlets 314 and 334. In FIG. 4, an extension length 440 defines a distance between the transition between gas inlets and the location of wall 302. In this
    P0017FI example, wall 302 extends into the bed solids within the volatilization stage 310 (upstream of the transition between stages). Wall 302 may extend into the bed solids within the combustion stage 330 (downstream of the transition).
    [0055] In some cases, the floor height of a stage is different than that of another stage, as shown in FIG. 4. A system may have a desired floor height difference 410 (typically controlled structurally/mechanically) and/or a desired bed surface height difference 420, typically controlled via pressure difference between the two beds. The extension distance of wall 302 into the bed, extension length 440, a distance 450 from the lower edge of the wall to the floor below, and/or the floor heights, may be used to define a transfer area 430 between the two beds. The transfer area may have a horizontal component (eg., allowing for vertical bed flow) and/or a vertical component (eg., allowing for horizontal bed flow), and is typically designed using Computational Fluid Design (CFD) tools to model bed flow and heat transfer between the stages. The transfer area is typically designed to achieve a desired heat and/or mass transfer between the beds (typically in concert with an expected pressure difference). Certain reactors include a stage having an adjustable floor height, which may provide independent pressure control (of the gas phases in the stages) and bed depths within each stage. Such control may be used to ensure both passage of the char stream from the first to second stage and recirculation of the bed media from the second to first stage.
    [0056] For example, extraction of a combustible gas produced from a combustible solid or liquid may implement a single fluidized bed reactor having multiple stages. A combustion stage, where part of the cross section of the reactor vessel is fluidized with air, may be preceded by a volatilization stage, in which extraction and/or reaction is performed in a secondary reactor volume in which the fuel residence time is controlled by adjusting the pressure difference between the stages. A pressure difference between the stages (P1-P2, FIG. 4) and the pressure drop relationships across the distributor plate and the fluidized bed beneath the second reactor volume ((Pd2-P2)/ (PaiPdz) FIG. 4) as well as the effective distance 450 (FIG. 4) between the distributor plate and the lower end wall 302 of the secondary reactor volume may be controlled. In some embodiments, an extracted volatiles stream has a lower heating value at least two times higher than the average heating value of the total gas volume leaving the volatilization and combustion stages.
    [0057] FIG. 5 illustrates a three-stage reactor with an internal wall separating the gas phases of the fuel inlet and volatiles outlet, per some embodiments. In this example, internal wall 402 extends into the bed of the volatilization stage, separating this stage into an
    P0017FI inlet stage 510 (in communication with the fuel inlet 316) and a reforming stage 610 (in communication with the volatiles outlet 318). Reforming stage 610 may be used for reforming reactions or other reactions. In descending below the surface of the bed, internal wall 402 forces all material (including gases) through the bed before volatiles may exit.
    [0058] The depth (into the bed) and thickness (in the flow direction) of the internal wall 402 may be chosen according to a desired residence time within the bed. FIG. 5 illustrates an additional pressure gauge 354 coupled to the controller, providing for separate pressure control over the inlet and reforming stages 510, 610 of the volatilization stage (e.g., via a separate valve 370' and/or gas inlet 316' providing for gas control into and/or out of inlet stage 510.
    [0059] In this example, a second fuel inlet 336 provides additional fuel for the third (combustion) stage, and all three stages having the same floor height. This example schematically illustrates increasingly higher pressures in stages 510, 610, and 330, resulting (in this case) in shorter distances between bed surface and floor. FIG. 5 illustrates differences 520, 520' between the surface heights of the beds of adjacent stages. The difference in heights of the bed surfaces may be controlled via corresponding pressure differences to achieve a desired flow rate (e.g., mass transfer equalization between fuel inlet 316, volatiles outlet 318, and exhaust 337. In this example, the stages have the same floor height (they may be different). In an embodiment, stages 510 and 610 have separate gas inlets and gas supplies (e.g., to deliver a different gas to the inlet stage than the reforming stage, which may be different than that delivered to the combustion stage. The distance from the lowermost edge of a wall to the bottom of a stage may be chosen according to a desired transfer area 430 (FIG. 4). In this example, a fan 338 is included to pump gas into or out of stage 510.
    [0060] FIG. 6 illustrates a three-stage reactor with an internal wall separating the gas phases of the fuel inlet and volatiles outlet, per some embodiments. In this example, wall 302 extends into the bed at the transition between the volatilization and combustion stages, and internal wall 402 separates the volatilization stage into an inlet stage 510 and a reforming stage 610.
    [0061] FIG. 6 illustrates a baffle 620 (in this example, disposed at the surface of the bed of the inlet stage 510. A baffle may be used to force non-gaseous fuel to pass
    P0017FI through the bed for a certain amount of time. Baffle 620 typically extends above the surface of the bed (e.g., above the bubble zone), such that fuel cannot pass over the baffle. Fuel must pass beneath the baffle to move from the portion of the bed in communication with the fuel inlet to the portion in communication with the volatiles outlet (and by extension, into the combustion stage). Baffle depth and thickness may be chosen according to a desired residence time in the bed. This example shows a constant floor height across the stages. A baffle may be used to segregate surface solids (e.g., incoming fuel), creating an internal dam (e.g., close to the fuel inlet) while keeping a portion of the bed open to the gas phase downstream of the baffle.
    [0062] Internal upgrading of a combustible gas produced from a combustible solid or liquid is possible after extraction from a first fluidized bed reactor stage, where part of the cross section of the reactor vessel is fluidized with air and the extraction is achieved by the introduction of a secondary (upstream) reactor stage in which the fuel residence time is controlled by adjusting the pressure difference between the stages and the pressure drop relation between the pressure drop across the distributor plate and the hydrostatic pressure at the bottom of the fluidized bed(s), as well as lengths, distances and areas (450,440,430 FIG. 4) between and among the distributor plate(s) and the wall separating the stages. In some embodiments, the extracted gas has a lower heating value at least two times higher than the average heating value of the total gas volume leaving the primary and secondary reactor volumes, and where the upgrading of the extracted gas is achieved by the introduction of a third stage within the volatilization stage (with or without a baffle) to force all extracted gas to pass through a controlled height of bed material before the extraction of the volatiles.
    [0063] Various features described herein may be implemented independently and/or in combination with each other. An explicit combination of features in an embodiment does not preclude the omission of any of these features from other embodiments. The above description is illustrative and not restrictive. Many variations of the invention will become apparent to those of skill in the art upon review of this disclosure. The scope of the invention should, therefore, be determined not with reference to the above description, but instead should be determined with reference to the appended claims along with their full scope of equivalents.
    权利要求:
    Claims (10)
    [1] 1. A fluidized bed reactor (300,400,500, 600) configured to react a fuel in a fluidized bed of bed solids, the reactor comprising:
    a container (301) configured to hold the bed of bed solids;
    a wall (302) separating the container (301) into a volatilization stage (310) and a combustion stage (330), the volatilization stage having:
    a fuel inlet (316) configured to receive the fuel;
    a gas inlet (314) disposed at a first portion of a bottom of the container;
    an inert gas supply (311) configured to supply hot inert and/or reducing gas to the inert gas inlets to fluidize the bed of bed solids and volatilize the fuel to yield a volatiles stream and a char stream;
    a volatiles stream outlet (318) configured to convey the volatiles stream out of the volatilization stage;
    a volatiles pressure gauge (350) configured to measure pressure within the volatilization stage; and the combustion stage having:
    an oxidant inlet (334) disposed at a second portion of the bottom of the container;
    an oxidant supply (331) configured to supply an oxidant, particularly air, to the oxidant inlet, the oxidant supply and oxidant inlet configured to fluidize the bed of bed solids and combust the char stream to yield an exhaust gas; and an exhaust gas outlet (337) configured to convey the exhaust gas out of the combustion stage; and a combustion pressure gauge (352) configured to measure pressure within the combustion stage;
    an opening (304) in the wall configured to provide for a flow of the char stream and bed solids from the volatilization stage to the combustion stage;
    a means to control gas flow into/out of at least one stage (310, 330), particularly a valve (370, 370'), a fan (338), gas inlet (314, 316'), and/or an oxidant inlet (333,334); and a controller (360) coupled to the pressure gauges (350, 352) and the means to control gas flow, the controller configured to control a pressure difference between the stages (310, 330), particularly to regulate the flow of char stream and bed solids from the volatilization stage to the combustion stage, particularly wherein the volatilization stage pressure is controlled to exceed the combustion stage pressure.
    P0017FI
    [2] 2. The reactor of claim 1, further comprising a heat exchanger (340) coupled to the exhaust gas outlet (337) and inert gas supply (311), the heat exchanger configured to transfer heat from the exhaust gas to the inert gas prior to the inert gas inlets.
    [3] 3. The reactor of either of claims 1 and 2, wherein the volatilization stage further comprises an internal wall (402) between the fuel inlet and volatiles stream outlet.
    [4] 4. The reactor of claim 3, wherein the internal wall (402) extends into the fluidized bed of bed solids in the volatilization stage (310).
    [5] 5. The reactor of any of claims 1-4, further comprising a baffle (620) disposed at a top surface of the fluidized bed of bed solids, particularly in the volatilization stage (310), particularly in an inlet stage (510) of the volatilization stage (310).
    [6] 6. The reactor of either of claims 4 and 5, wherein:
    the internal wall (402) separates the volatilization stage (310) into an inlet stage (510) and a reforming stage (610);
    the pressure gauge (350) and volatiles stream outlet (318) are disposed in the reforming stage (610);
    the reactor further comprises an inlet pressure gauge (354) coupled to the controller (360) and configured to measure pressure within the inlet stage (510); and the controller (360) is configured to independently control the pressures within the inlet stage (510) and the reforming stage (610).
    P0017FI
    [7] 7. A fuel processing system comprising:
    the reactor of any of claims 1-6; and a separation reactor (220) coupled to the volatiles stream outlet (318) and configured to receive the volatiles stream from the volatilization stage, particularly wherein the separation reactor comprises at least one of a heat exchanger, a condenser, a separator configured to separate two phases or species, and a cyclone.
    [8] 8. A method comprising:
    providing a fluidized bed reactor according to any of claims 1-6;
    delivering a fuel comprising at least one of wood, straw, garbage, MSW, and sewage to the volatilization stage;
    delivering an inert and/or reducing gas to the volatilization stage to fluidize the bed of solids and at least partially volatilize the fuel;
    delivering an oxidizing gas to the combustion stage to combust the char stream; and controlling a residence time of the fuel in the volatilization stage and/or a flow of the char stream and bed solids from the volatilization stage to the combustion stage by controlling a pressure difference between the volatilization stage and the combustion stage.
    P0017FI
    [9] 9. A fuel stream processing system (200) comprising:
    a pretreatment reactor (210) including:
    a reaction zone (212), particularly a fluidized bed reactor, configured to react the fuel stream with an inlet gas;
    a gas inlet (214) configured to deliver an inert or reducing inlet gas into the reaction zone;
    a fuel inlet (216) configured to receive a fuel supply, particularly a granular fuel supply, particularly a fuel supply comprising at least one of biomass, MSW, and sewage and deliver the fuel supply to the reaction zone;
    a volatiles stream outlet (218) configured to convey a volatiles stream out of the reaction zone; and a char stream outlet (219) configured to convey a char stream out of the reaction zone;
    a separation reactor (220), particularly a fast condensation reactor, comprising:
    a volatiles stream inlet (222) fluidically coupled to the volatiles stream outlet and configured to receive the volatiles stream from the pretreatment reactor;
    a volatiles heat exchanger (224) configured to cool the volatiles stream into at least one condensed species and a residual stream; and a phase separator (226) configured to separate the condensed species from the residual stream; and a residual stream outlet (228) configured to convey the residual stream out of the separation reactor; and a combustion reactor (230), particularly a CHP plant, comprising:
    a combustion zone (232), particularly a fluidized bed combustor, an oxidant inlet (234) configured to deliver an oxidant, particularly air, to the combustion zone;
    a char stream inlet (239) coupled to the char stream outlet of the pretreatment reactor and configured to convey the char stream into the combustion zone;
    a residual stream inlet (238) coupled to the residual stream outlet of the separation reactor and configured to deliver the residual stream into the combustion zone; and an exhaust outlet (237) configured to convey an exhaust from the combustion of the oxidant, char stream, residual stream, and optionally a second fuel supplied to the combustion reactor, out of the combustion zone.
    P0017FI
    [10] 10. The fuel stream processing system of claim 9, wherein:
    the pretreatment reactor (210) of the fuel stream processing system (200) is configured as the volatilization stage (310, 510, 610) of the fluidized bed reactor (300, 400, 500, 600) of any of claims 1-6; and the combustion reactor (230) of the fuel stream processing system is configured as the combustion stage (330) of the fluidized bed reactor of any of claims 1-6, such that the wall (302) separates the pretreatment reactor from the combustion reactor and the opening (304) provides for the flow of char stream and bed solids from the pretreatment reactor to the combustion reactor.
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    公开号 | 公开日
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    EP3688372A2|2020-08-05|
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    优先权:
    申请号 | 申请日 | 专利标题
    US201762517186P| true| 2017-06-09|2017-06-09|EP18739642.9A| EP3688372A2|2017-06-09|2018-06-11|Fluidized bed reactor and method using the same|
    US16/620,510| US20200141570A1|2017-06-09|2018-06-11|Recovery of chemicals from fuel streams|
    PCT/IB2018/054189| WO2018225047A2|2017-06-09|2018-06-11|Bubbling fluidized bed reactor with circulation among integrated bubbling zones|
    PCT/IB2018/054187| WO2018225046A2|2017-06-09|2018-06-11|Recovery of chemicals from fuel streams|
    EP18830946.2A| EP3803206A1|2017-06-09|2018-12-09|Spray, jet, and/or splash induced circulation among integrated bubbling zones in a bubbling fluidized bed reactor|
    SE2030362A| SE2030362A1|2017-06-09|2018-12-09|Spray, jet, and/or splash induced circulation among integrated bubbling zones in a bubbling fluidized bed reactor|
    PCT/IB2018/059806| WO2019239209A1|2017-06-09|2018-12-09|Spray, jet, and/or splash induced circulation among integrated bubbling zones in a bubbling fluidized bed reactor|
    SE2030363A| SE2030363A1|2017-06-09|2019-06-07|Fuel Processing system|
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