EP4209710A1 - Unité de lit fluidisé - Google Patents
Unité de lit fluidisé Download PDFInfo
- Publication number
- EP4209710A1 EP4209710A1 EP22020003.4A EP22020003A EP4209710A1 EP 4209710 A1 EP4209710 A1 EP 4209710A1 EP 22020003 A EP22020003 A EP 22020003A EP 4209710 A1 EP4209710 A1 EP 4209710A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- fluidised bed
- cylinder
- bed unit
- fluidised
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 239000002245 particle Substances 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 20
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 17
- 239000003546 flue gas Substances 0.000 claims abstract description 17
- 230000003197 catalytic effect Effects 0.000 claims abstract description 13
- 238000005243 fluidization Methods 0.000 claims abstract description 11
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 8
- 239000002699 waste material Substances 0.000 claims abstract description 7
- 238000004880 explosion Methods 0.000 claims abstract description 6
- 239000006227 byproduct Substances 0.000 claims abstract description 4
- 238000007669 thermal treatment Methods 0.000 claims abstract description 4
- 239000002028 Biomass Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 24
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 238000002347 injection Methods 0.000 claims description 2
- 239000007924 injection Substances 0.000 claims description 2
- 229910052609 olivine Inorganic materials 0.000 claims description 2
- 239000010450 olivine Substances 0.000 claims description 2
- 239000004576 sand Substances 0.000 claims description 2
- 239000010802 sludge Substances 0.000 claims 1
- 238000009434 installation Methods 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 8
- 238000012545 processing Methods 0.000 abstract description 6
- 239000010801 sewage sludge Substances 0.000 abstract 1
- 230000005587 bubbling Effects 0.000 description 13
- 239000007787 solid Substances 0.000 description 13
- 239000000463 material Substances 0.000 description 9
- 238000000034 method Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 7
- 239000002956 ash Substances 0.000 description 6
- 239000000446 fuel Substances 0.000 description 5
- 238000002309 gasification Methods 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000001816 cooling Methods 0.000 description 3
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 2
- 238000003763 carbonization Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000011343 solid material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000001033 granulometry Methods 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000155 melt Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000005979 thermal decomposition reaction Methods 0.000 description 1
- 230000000930 thermomechanical effect Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000002916 wood waste Substances 0.000 description 1
Images
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/005—Fluidised bed combustion apparatus comprising two or more beds
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
Definitions
- This invention relates to an improved small and medium scale fluidised bed reactor that can be equipped with an internal catalytic filter suitable for factory skid mounting and for site treatment of small and medium quantity of feedstock.
- Fluidised bed units are commonly used in large scale incineration plants and are typically very large, bulky machines with typical height higher than 6m and horizontal dimensions larger than three meters.
- the known fluidised bed units are operated to thermally treat coal, waste or other like material in incineration plants.
- a problem with the known fluidised bed units is that they are very large, expensive machines that are only suitable for large scale combustion or incineration plants with a plentiful supply of feedstock.
- Another problem with the fluidised bed units is that they require constant surveillance and frequent maintenance by skilled personnel to ensure optimal operation.
- the known fluidised bed units are therefore time consuming and costly to operate as well as being unsuitable for small scale installations such as processing plants.
- the present invention is concerned with relatively small installations capable of handling up to 3MW thermal and up to 1000kg/h of feedstock.
- a fluidised bed reactor easily permits process scale, has a great processing capacity and good control of the process temperature. It also allows the addition of catalyst in the bed to improve process performance.
- fluidised bed reactors require a specific granulometry, homogeneity and specific preparation of the feedstocks. Sintering and agglomeration of the bed can result because of the thermo mechanical properties of the material and the melting temperature of the ashes.
- fluidised bed reactors can be bubbling or circulating.
- a bubbling fluidised bed reactor consists of a silica sand or similar material bed, fluidised by a gaseous stream coming from the bottom of the bed.
- the bubbling regime is characterised by formation and coalescence of bubbles causing solid mixing.
- the minimum velocity at which bubbles form is known as minimum fluidisation velocity.
- Use of bubbling fluidised bed reactors are well known for heat treating, of biomass, waste, coal, or other by-products with the objective, for example, of drying, thermal decomposition or combustion.
- the speed of thermal reactions depends on the operating conditions and fluidisation level across the entire bed.
- the air flow rate is normally of the order of 1 m/s.
- the solid matter concentration is low in the gas flow above a clearly limited bubbling fluidised bed.
- Temperature reactor space above the fluidised bed in a bubbling bed reactor can be raised by additional air supply or reduced by injecting cooling water into the gas flow.
- dust particles present in the gas flow can be separated with a distinct cyclone, in which the particles are returned to the bottom of the reactor space.
- "Winkler gasifiers" of this type are described in documents DE2751911 and DE19548324 .
- the fluidised particles are entrained by the product gas in the cyclone, in which the particles and the carbonisation residue derived from the fuel are separated and returned to the bottom of the reactor space.
- the circulating fluidised bed reactors have been given a height substantially greater than that of the bubbling fluidised bed reactors.
- Other typical properties of circulating fluidised beds comprise uniform temperature and relatively uniform viscosity of the solid matter suspension in the reactor space, without a clearly limited fluidised bed characteristic of bubbling fluidised beds.
- a typical fuel gasification process based on circulating fluidised bed reactors is disclosed in F162554.
- the reactor system comprising: a fluidised bed reactor chamber, a particle separator connected to the reactor chamber, for separating solid material from exhaust gases.
- a gas cooler having cooling surfaces is connected to the particle separator.
- means are provided for branching off a flow of solid bed material from the material separated in the particle separator and for introducing said branched off flow of bed material into the gas cooler.
- a flow of bed material is branched off from the main flow of solid particles, before or after discharging said first flow of solid particles from the particle separator. The branched off flow of solid particles are introduced into the gas discharged from the separator during, or before cooling of the gas, so that these particles mechanically dislodge deposits from cooling surfaces.
- a fluidised-bed furnace has an approximately circular horizontal cross-sectional configuration.
- a moving bed in which a fluidised medium settles and diffuses, is formed in the central portion of the furnace, and a fluidised bed, in which the fluidised medium is actively fluidised, is formed in the peripheral portion in the furnace.
- the fluidised medium is turned over to the upper part of the moving bed from the upper part of the fluidised bed, thus circulating through the two beds.
- Combustible matter is cast into the upper part of the moving bed and gasified to form a combustible gas while circulating, together with the fluidised medium.
- the amount of oxygen supplied to the fluidised-bed furnace is set so as to be the same contained in an amount of air not higher than 30% of the theoretical amount of combustion air.
- the temperature of the fluidised bed is maintained at 450 °C to 650 °C so that the combustible gas produced contains a large amount of combustible component.
- the combustible gas and fine particles produced in the fluidised-bed furnace are supplied to a melt combustion furnace where they are burned at high temperature, and the resulting ash is melted.
- EP0433547 refers to an apparatus to gasify solid fuels, which consists of a gas producer having a pre-charging silo, a carbonisation or coking and gasification silo and a furnace and is particularly suitable to gasify low cost products such as wood waste and chips, solid biomasses in general, tyres, peat, lignite, coal and other materials, and advantageously solid urban wastes, a direct flame or flames and a downward flame or flames being included in the furnace of the gas producer.
- a gas producer having a pre-charging silo, a carbonisation or coking and gasification silo and a furnace and is particularly suitable to gasify low cost products such as wood waste and chips, solid biomasses in general, tyres, peat, lignite, coal and other materials, and advantageously solid urban wastes, a direct flame or flames and a downward flame or flames being included in the furnace of the gas producer.
- European patent EP1432779 refers to a method and apparatus for gasifying fuel in a fluidised bed reactor containing fluidised solid material particles.
- the fuel is introduced into the reactor bottom part, and product gas formed in gasification is led from the reactor top to a separator, such as a cyclone, which separates solid particles from the gas for recirculation to the reactor.
- a separator such as a cyclone
- a bubbling fluidised bed containing coarser particles and above this, a circulating bed containing finer particles are maintained in the reactor by recirculating the particles separated from the product gas to the reactor, to the top of the bubbling fluidised bed or above this.
- the reactor may comprise a lower part for the bubbling fluidised bed and an upper part larger in cross-section for the circulating fluidised bed, the speed of the ascending gas flow in the circulating bed being equal to or lower than that of the bubbling bed.
- the separating limit in the cyclone may be adjusted such that the discharged product gas flow entrains solid particles, which have a binding effect on tacky ash particles.
- the product gas is cooled in two successive heat exchangers before filtration of the gas.
- the method is suitable for gasification of biomasses and recycled fuels forming tars and/or containing chlorine, thus providing a solution to the problems of fouled and clogged gas ducts.
- State of the art systems are very tall to limit the entrained particles and to allow the residence time required to complete the expected reactions.
- the height of state-of-the-art systems does not allow factory skid mounting because of the limited height and horizontal dimensions permitted for transportation. None of the state-of-the-art systems is equipped with internal devices for effective trapping and possible catalytic post treatment of flue gas and products that are entrained from the bed.
- the present invention allows the required residence time with a limited height compatible with factory skid mount significantly reducing installation cost. It also permits a precise flue gas temperature control downstream from the bed and effective internal filtering and catalytic processing of the flue gas.
- a fluidised bed reactor that comprises three cylinders arranged in an inverted "U" shape, hereafter described, is disclosed.
- the first cylinder is vertical and comprises a feedstock inlet, a fluidisation agent inlet, a nozzles inlet box, a plurality of nozzles for injecting the fluidisation agent in the bed, a plurality of temperature and pressure sensors.
- the flow in the first cylinder is upward.
- the second cylinder is horizontal and comprises a flue gas temperature control device and an explosion protection device.
- the flow in the second cylinder is horizontal moving from the first cylinder toward the third cylinder.
- the third cylinder is vertical and comprises a temperature control device, a catalyst filter, an auger for feeding new catalyst and extracting exhausted catalyst and trapped particles, a plurality of temperature and pressure sensors. The flow in the third cylinder is downward.
- the fluidised bed unit is compact, relatively simple to maintain and commercially viable so that it may be skid mounted in the factory and transported to the installation site.
- the fluidised bed unit can also be part of an energy conversion system that is suitable for installation on small and medium scale processing plants.
- the system is characterised by an inverted 'U' shape in which the flue gas flow is first upward, then horizontal and finally downward.
- Such arrangement allows to accomplish the necessary residence time to complete the reactions with a lower height than prior art systems, it can also allow temperature control in the freeboard, effective entrained ash and particle removal and a catalytic flue gas post processing with the internal catalytic filter.
- a fluidised bed reactor for thermal treatment of biomasses, waste, by-products in general and for any known application involving fluidised bed reactors, in accordance with the preferred embodiment of the present invention, comprises a nozzle inlet box 1, a plurality of fluidisation agent injection nozzles 2, a bed of olivine or similar material 3, an upward flow cylinder 4, a horizontal cylinder 5 equipped with a temperature control device 6, a downward flow cylinder 7, a catalyst filter comprising a catalytic bed 10, an outer cylinder 16 and an inner cylinder 18, a catalyst and trapped solid particles extraction device 9, an explosion protection device 15, a feedstock inlet 12 and a flue gas outlet 11.
- the fluidisation agent enters the system through the inlet flange 14 pressurising the nozzle inlet box 1.
- the nozzle inlet box 1 acts as a pressure dampener so that the pressure upstream each nozzle 2 is the same and thus the fluidisation agent velocity entering the reactor 4, allowing consistent fluidisation regime across the bed. Reactions start in the bed 3 and continue in the first, second and third cylinder.
- the horizontal cylinder 5 is equipped with an explosion protection device, such as a hydraulic seal 15 or an equivalent device, a temperature control device 6, allowing water to be sprayed to decrease, or injecting air to increase, flue gas temperature.
- the third downward flow cylinder 7 is equipped with a temperature control device 13 and with the catalytic filtration system detailed in the Fig. 5 .
- the catalytic filtration system is composed by cylinders 16 and 17.
- the catalyst bed 10 is positioned in the space between cylinder 7 and cylinder 16 and in the space between cylinder 16 and cylinder 17.
- the flue gas passes through the catalyst bed 10 in downward direction in the space between the cylinder 7 and the cylinder 16 and in upward direction in the space between cylinder 16 and cylinder 17.
- flue gas passes through the holes 18 and flows in downward direction inside the cylinder 17 and eventually exits the system through the outlet 11.
- the auger 9 allows removal of exhausted catalyst, ashes and trapped particles collected through the outlet 19 and addition of fresh catalyst via the inlet 20.
- Fig. 7 the preferred embodiment of a skid mount of a complete system including the fluidised bed reactor, a flue gas clean-up section and fans is disclosed.
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP22020003.4A EP4209710A1 (fr) | 2022-01-10 | 2022-01-10 | Unité de lit fluidisé |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP22020003.4A EP4209710A1 (fr) | 2022-01-10 | 2022-01-10 | Unité de lit fluidisé |
Publications (1)
Publication Number | Publication Date |
---|---|
EP4209710A1 true EP4209710A1 (fr) | 2023-07-12 |
Family
ID=80112023
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP22020003.4A Withdrawn EP4209710A1 (fr) | 2022-01-10 | 2022-01-10 | Unité de lit fluidisé |
Country Status (1)
Country | Link |
---|---|
EP (1) | EP4209710A1 (fr) |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2751911A1 (de) | 1977-11-21 | 1979-05-23 | Davy Powergas Gmbh | Verfahren und vorrichtung fuer die vergasung von kohlenstaub |
EP0433547A1 (fr) | 1989-11-29 | 1991-06-26 | SAS GINO TOMADINI & C. | Appareil pour gazéifier des combustibles solides |
US5462718A (en) * | 1994-06-13 | 1995-10-31 | Foster Wheeler Energy Corporation | System for decreasing NOx emissions from a fluidized bed reactor |
DE19548324A1 (de) | 1994-12-23 | 1996-06-27 | Rheinische Braunkohlenw Ag | Verfahren zum Vergasen von kohlenstoffhaltigen Feststoffen in der Wirbelschicht sowie dafür verwendbarer Vergaser |
EP0889943A1 (fr) | 1996-02-21 | 1999-01-13 | Foster Wheeler Energia Oy | Systeme de reacteur a lit fluidise et procede d'exploitation |
WO2001033140A1 (fr) * | 1999-11-02 | 2001-05-10 | Consolidated Engineering Company, Inc. | Procede et appareil permettant la combustion du charbon residuel contenu dans des particules de cendres volantes |
EP1286113A2 (fr) | 1994-03-10 | 2003-02-26 | Ebara Corporation | Méthode et appareil pour la gazéification en lit fluidisé et combustion dans un lit à fusion |
EP1432779A1 (fr) | 2001-10-02 | 2004-06-30 | Valtion Teknillinen Tutkimuskeskus | Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise |
US20140008205A1 (en) * | 2010-09-10 | 2014-01-09 | University Of Pretoria | Fluidised bed pyrolysis apparatus and method |
-
2022
- 2022-01-10 EP EP22020003.4A patent/EP4209710A1/fr not_active Withdrawn
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2751911A1 (de) | 1977-11-21 | 1979-05-23 | Davy Powergas Gmbh | Verfahren und vorrichtung fuer die vergasung von kohlenstaub |
EP0433547A1 (fr) | 1989-11-29 | 1991-06-26 | SAS GINO TOMADINI & C. | Appareil pour gazéifier des combustibles solides |
EP1286113A2 (fr) | 1994-03-10 | 2003-02-26 | Ebara Corporation | Méthode et appareil pour la gazéification en lit fluidisé et combustion dans un lit à fusion |
US5462718A (en) * | 1994-06-13 | 1995-10-31 | Foster Wheeler Energy Corporation | System for decreasing NOx emissions from a fluidized bed reactor |
DE19548324A1 (de) | 1994-12-23 | 1996-06-27 | Rheinische Braunkohlenw Ag | Verfahren zum Vergasen von kohlenstoffhaltigen Feststoffen in der Wirbelschicht sowie dafür verwendbarer Vergaser |
EP0889943A1 (fr) | 1996-02-21 | 1999-01-13 | Foster Wheeler Energia Oy | Systeme de reacteur a lit fluidise et procede d'exploitation |
WO2001033140A1 (fr) * | 1999-11-02 | 2001-05-10 | Consolidated Engineering Company, Inc. | Procede et appareil permettant la combustion du charbon residuel contenu dans des particules de cendres volantes |
EP1432779A1 (fr) | 2001-10-02 | 2004-06-30 | Valtion Teknillinen Tutkimuskeskus | Procede et appareil pour la gazeification de combustible dans un reacteur a lit fluidise |
US20140008205A1 (en) * | 2010-09-10 | 2014-01-09 | University Of Pretoria | Fluidised bed pyrolysis apparatus and method |
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