EP0304111A1 - Méthode de mise en oeuvre de processus exothermiques - Google Patents

Méthode de mise en oeuvre de processus exothermiques Download PDF

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Publication number
EP0304111A1
EP0304111A1 EP88201643A EP88201643A EP0304111A1 EP 0304111 A1 EP0304111 A1 EP 0304111A1 EP 88201643 A EP88201643 A EP 88201643A EP 88201643 A EP88201643 A EP 88201643A EP 0304111 A1 EP0304111 A1 EP 0304111A1
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EP
European Patent Office
Prior art keywords
fluidized bed
bed reactor
mixing chamber
gas
fuel
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.)
Granted
Application number
EP88201643A
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German (de)
English (en)
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EP0304111B1 (fr
Inventor
Hans Beisswenger
Alexander Teodor Wechsler
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GEA Group AG
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Metallgesellschaft AG
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Priority to AT88201643T priority Critical patent/ATE68578T1/de
Publication of EP0304111A1 publication Critical patent/EP0304111A1/fr
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    • 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
    • F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
    • F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
    • F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
    • F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
    • 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 
    • F23C2206/00—Fluidised bed combustion
    • F23C2206/10—Circulating fluidised bed
    • F23C2206/101—Entrained or fast fluidised bed

Definitions

  • the invention relates to a method for carrying out exothermic processes with near-stoichiometric combustion of the combustible constituents of the feed materials in a fluidized bed reactor with a circulating fluidized bed in which solids circulate through a circulation system formed from a fluidized bed reactor, separator and return line and in which the combustion with at least two at different levels supplied partial streams of oxygen-containing gases is carried out.
  • the basic method is described in DE-PS 25 39 546 (corresponding to US Pat. No. 4,165,717) especially for combustion processes. It provides for the combustion to be carried out in two stages and to remove the heat of combustion with the aid of cooling surfaces which are arranged above the secondary gas supply in the fluidized bed reactor.
  • the particular advantage of the method is that the combustion process can be adapted to the power requirement in a technically simple manner by regulating the suspension density and thus the heat transfer to the cooling surfaces in the upper reactor space.
  • the object of the invention is to provide a process for carrying out exothermic processes with near-stoichiometric combustion of the combustible constituents of the materials given in a circulating fluidized bed, which avoids the disadvantages of the known processes and in particular enables the concentration profile of the solid to be set correctly in a process-related and apparatus-simple manner .
  • the object is achieved in that the method of the type mentioned is designed in accordance with the invention in such a way that solids are removed from the separator or the return line, introduced into a mixing chamber, mixed there with fuel and fluidized with gas, which is obtained by fluidizing the coarse grain separated fine grain at least partially and the fluidizing gas completely feeds the fluidized bed reactor and discharges coarse grain from the mixing chamber.
  • the measure of fluidization in the mixing chamber according to the invention makes it possible to largely separate fine grain from coarse grain, so that the coarse grain mentioned in the description of the problem of setting a suitable solid profile does not even occur in the fluidized bed reactor.
  • the gas used in the mixing chamber can be low-air or low-oxygen gas. However, it is also suitable Inert gas. It is particularly advantageous to carry out the fluidization of the removed solid and fuel in the mixing chamber with flue gas. It is important to ensure that the flue gas is dedusted as much as possible before it is fed into the mixing chamber. The use of flue gas has the advantage that combustion of the fuel introduced into the mixing chamber and the associated risk of local overheating is avoided.
  • the coarse grain discharged from the lower area of the mixing chamber is cooled and ground as required and fed back to the fluidized bed reactor.
  • the fine grain found in the upper area of the mixing chamber is returned to the fluidized bed reactor.
  • the mixing chamber fluidized with gas can be designed in different ways. It is particularly advantageous to mix the removed solid and fuel in a mixing chamber designed as a dip pot.
  • a dip pot is a U-shaped closure, one leg of which receives the solid flowing in from the return cyclone and the other leg causes the solid to be carried further into the return line or into the fluidized bed reactor.
  • the immersion pot is flown with fluidizing gas.
  • this mixing chamber in the form of a dip pot has additional device elements which allow the fuel to be introduced and the coarse grain to be discharged.
  • the mixing of removed solid and fuel can be carried out in a fluidized bed cooler or its prechamber free of cooling surfaces.
  • the cooler can be a structurally separate device, and the fluidized bed cooler with the fluidized bed reactor also has a common wall.
  • the cooler or its prechamber has additional device elements for the introduction of fuel and the discharge of coarse particles.
  • the fuel has to be introduced in such a way that gas forming by mixing can only move in the direction of the fluidized bed reactor, i.e. that a backflow e.g. towards the return cyclone is excluded.
  • a particularly effective separation between coarse and fine grain can be achieved if the fluidization of solid and fuel in the mixing chamber is carried out with gas supplied on two different levels.
  • a particularly advantageous separation can be achieved by suitable metering of the gas streams.
  • the mixing of fuel and solid in the mixing chamber causes the fuel to pre-dry; under certain conditions, partial smoldering or - when using oxygen-containing gases - partial gasification can also take place.
  • Another advantageous embodiment of the invention provides that the fine grain separated from the coarse grain is cooled in a fluidized bed cooler before being introduced into the fluidized bed reactor.
  • the method according to the invention would be integrated into the concept of carrying out exothermic processes according to DE-PS 26 24 302.
  • the method according to the invention can also be combined with the method according to DE-PS 25 39 546. Both of the aforementioned methods are included in the description with regard to their disclosure content.
  • fine grain used in connection with the present invention is generally understood to mean a grain with a particle diameter of less than 1 mm and with coarse grain particles with a grain size of more than 1 mm.
  • coarse grain particles When transporting, cooling, possibly screening and grinding the coarse grain, it is advisable to work with encapsulated and possibly under-pressure devices, since the coarse grain usually contains sulfur compounds that can emit undesired gases when moisture enters.
  • the principle of the circulating fluidized bed used in the invention is characterized in that that - in contrast to the "classic" fluidized bed, in which a dense phase is separated from the gas space above by a clear density jump - there are distribution states without a defined boundary layer. A leap in density between the dense phase and the dust space above it does not exist; however, the solids concentration within the reactor decreases continuously from bottom to top.
  • u the relative gas velocity in m / s Ar is the Archimedes number
  • ⁇ g is the density of the gas in kg / m3
  • ⁇ k is the density of the solid particle in kg / m3
  • d k is the diameter of the spherical particle in m
  • the kinematic toughness in m2 / s g is the gravitational constant in m / s2
  • the exothermic reaction is carried out at least in two stages with oxygen-containing gases supplied at different levels.
  • Their advantage lies in a "soft" implementation, in which local overheating phenomena are avoided and NO x formation is largely suppressed.
  • the upper supply point for oxygen-containing gas should be so far above the lower one that the oxygen content of the gas supplied at the lower point has already been largely consumed.
  • an advantageous embodiment of the invention consists in creating a certain average suspension density above the upper gas supply by adjusting the fluidization and secondary gas quantities and the heat of reaction by in the free space of the fluidized bed reactor above the uppermost secondary gas supply and / or on the wall to remove arranged heating surfaces of the fluidized bed reactor.
  • the gas velocities prevailing in the fluidized bed reactor above the secondary gas supply are usually above 5 m / s at normal pressure and can be up to 15 m / s, and the ratio of the diameter to the height of the fluidized bed reactor should be chosen such that gas residence times of 0.5 to 8 , 0 s, preferably 1 to 4 s, are obtained.
  • a plurality of supply openings for secondary gas are advantageous within each entry level.
  • the advantage of this mode of operation is in particular that a change in the production of the process heat quantity is possible in the simplest way by changing the suspension density in the furnace space of the fluidized bed reactor located above the secondary gas supply.
  • a certain heat transfer is associated with a prevailing operating state under predetermined fluidizing gas and secondary gas volumes and the resulting, certain, average suspension density.
  • the heat transfer to the cooling surfaces can be increased by increasing the suspension density by increasing the amount of fluidizing gas and possibly also the amount of secondary gas. With the increased heat transfer at a practically constant combustion temperature, it is possible to dissipate the heat generated at increased combustion output Given amounts of heat.
  • the increased oxygen requirement required due to the higher combustion output is here virtually automatically due to the higher fluidization gas used to increase the suspension density and possibly secondary gas quantities.
  • the combustion output can be regulated by reducing the suspension density in the furnace space of the fluidized bed reactor located above the secondary gas line. By lowering the suspension density, the heat transfer is also reduced, so that less heat is removed from the fluidized bed reactor.
  • the combustion performance can be reduced essentially without a change in temperature.
  • Another expedient, universally applicable embodiment of the invention consists in carrying out the process with at least one fluidized bed cooler connected via solid feed and solid return lines.
  • a certain suspension density is set above the upper secondary gas supply by suitable control of the fluidization and secondary gas quantities, hot solids are removed from the circulating fluidized bed, cooled in the fluidized state by direct and indirect heat exchange, and at least a partial stream of cooled solids is returned to the circulating fluidized bed.
  • the constant temperature can be achieved practically without changing the operating conditions in the fluidized bed reactor, i.e. without changing the suspension density, among other things, only by controlled removal of hot solid and controlled recycling of the cooled solid.
  • the recirculation rate is more or less high.
  • the temperatures can be set as desired from very low temperatures, which are close above the ignition limit, to very high temperatures, which are limited, for example, by softening the reaction residues. They can be between 450 and 950 ° C.
  • the temperature in the fluidized bed reactor is controlled by recirculating at least a partial stream of cooled solid from the fluidized bed cooler.
  • the required partial flow of cooled solid can be entered directly into the fluidized bed reactor.
  • the exhaust gas can also be cooled by introducing cooled solid matter, which is, for example, given to a pneumatic conveyor line or a floating exchanger stage, the solid matter which is subsequently separated off from the exhaust gas then being returned to the fluidized bed cooler.
  • the exhaust gas heat ultimately ends up in the fluidized bed cooler. It is particularly advantageous to enter cooled solid as a partial stream directly and as another indirectly after cooling the exhaust gases in the fluidized bed reactor.
  • the recooling of the hot solid of the fluidized bed reactor should take place in a fluidized bed cooler with several cooling chambers flowing through one after the other, into which interconnected cooling registers are immersed, in countercurrent to the coolant. This makes it possible to bind the heat of combustion to a comparatively small amount of coolant.
  • Another embodiment with a connected fluidized bed cooler is to connect it to the fluidized bed reactor to form a structural unit.
  • the The fluidized bed reactor and the fluidized bed cooler have a common, expediently cooled wall, which has a passage opening for cooled solid matter in the fluidized bed reactor.
  • the fluidized bed cooler can have several cooling chambers, but it can also consist of several units equipped with cooling surfaces, each of which has a common wall with the fluidized bed reactor with a passage opening for solids and its own solids supply line. Such a device is described in EP-A-206 066.
  • air or oxygen-enriched air or technically pure oxygen can be used as the oxygen-containing gases for supplying the fluidized bed reactor.
  • an increase in performance can be achieved if the reaction is carried out under pressure, for example up to 20 bar.
  • all self-combustible materials can be treated with the method according to the invention.
  • examples are all types of coal, especially those of lower quality, such as coal washing mountains, mud coal, coal with a high salt content, but also lignite and Oil shale. It can also be used to roast sulfide ores or ore concentrates.
  • a fluidized bed reactor 10
  • the exhaust gas is fed via line (12) together with suspended solids into a recycle cyclone (14), in which the bulk of the discharged solids is separated from the gas.
  • the gas freed from the bulk of the solid passes through line (16) through a waste heat boiler (not shown) and then into a gas cleaning device, for example into a electrostatic gas cleaning or a cloth filter where the remaining solid particles are separated.
  • the solid separated in the return cyclone is introduced via a line into the mixing chamber (18), into which the carbon-containing material is added with the aid of a feed device (20).
  • the hot solid can be introduced directly into the mixing chamber (18) from the lower region of the return cyclone (14). In such a case, it is necessary to create a lock-like lock using a material column. However, a pendulum flap can also be provided in the lower cyclone area, it being possible to dispense with the aforementioned material column as a lock. In any case, it is necessary to create a barrier that prevents gas from flowing in the wrong direction.
  • Cleaned flue gas is fed via line (22) to the mixing chamber (18) as fluidizing gas.
  • air or inert gas or low-oxygen gases are also suitable.
  • the flue gas is introduced into the mixing chamber (18) at least at one point through inlet openings (24). However, it is also possible to additionally enter the flue gas at a second higher level (26). The introduction of flue gas creates two different fluidization zones in the mixing chamber (18).
  • At least part of the fine grain is introduced via line (28) from the mixing chamber (18) into the fluidized bed reactor (10) below the secondary gas line.
  • a other part of the fine material can be fed into an external fluidized bed cooler (25), in which it partially emits its sensible heat.
  • the cooled fine grain can then be returned to the fluidized bed reactor (10).
  • At least part of the coarse grain is discharged from the mixing chamber (18) through line (30) and cooled.
  • the cooling takes place in the device (32), which is preferably designed as a screw heat exchanger.
  • the cooled solid is then passed through a transport device (34) and separated in a sieve device (36) into a fraction of less than 1 mm and one larger than 1 mm.
  • the fraction with a grain size of less than 1 mm arrives in a storage container (38), the coarse grain is ground in a device (40) in such a way that a grain with a grain size of less than 1 mm is also formed, which is also in the storage container (38) reached.
  • the part of ground solid that is required in each case is returned to the fluidized bed reactor (10) below the secondary air supply by means of discharge device (42) and line (44).
  • FIG. 2 shows a preferred embodiment of the mixing chamber (18).
  • the mixing chamber (18) is provided with a fuel entry (48).
  • the grate of the mixing chamber (18) is labeled (50). Gas under pressure is introduced through the grate (50) into the lower region of the mixing chamber (18) via the collecting line (52) and the pipes (54).
  • a line (56) leads the fine grain separated by fluidization into the fluidized bed reactor (10).
  • the mixing chamber (18) is further provided with an extraction device (58) through which coarse grain can be removed.
  • the mixing chamber (18) can also be provided with entry devices (60) through which the supply of secondary gas is possible. The height of the secondary gas supply has a significant influence on the interface of the fluidization zones of coarse and fine particles.
  • the entry devices (60) must not be higher than the lower part (62) of the connecting line (56). Solid can be discharged into a fluidized bed cooler (25) by means of a discharge device (63) which may be present.
  • the mixing chamber (18) is equipped with dividing walls (51) and (53), the arrangement of which is selected in such a way that a material column acting as a lock, which prevents the breakthrough of gas in the direction of the return cyclone, can form.
  • FIG. 3 shows another embodiment of the mixing chamber (18), which has a grate (50), manifolds (52) and fluidizing gas feeds (54).
  • (62) the lower wall of the solid line (56), which causes fine grain to pass from the mixing chamber (18) into the fluidized bed reactor (10), is shown.
  • the fuel input is again identified with (48).
  • the mixing chamber (18) of FIG. 3 has a mixing chamber section (64) which tapers upwards.
  • the entry of secondary gas at a level above the grate is not necessary.
  • the cross section narrowing upward the gas velocity increases upward so that a first and a second vortex zone can also form in this embodiment.
  • These two zones are labeled (66) and (68).
  • Zone 66 The velocity of the fluidizing gas in the lower zone of the mixing chamber (18) (zone 66) is of the order of about 0.1 to 1 m / sec.
  • the speed of the fluidizing gas in the upper part of the upper zone (68) is approximately 0.5 to 5 m / sec.
  • Zone (66) essentially contains coarse grain with a grain size greater than 1 mm, whereas zone (68) has fine grain with a grain size less than 1 mm.
  • An energy generation system operated according to the method according to the invention is designed for an output of 80 MW el .
  • 800 to 1000 t of solid, which essentially consists of ash are discharged at a temperature of 850 ° C. per hour and transferred to the mixing chamber (18).
  • the mixing chamber (18) is also supplied with 20 t / h of fuel, which is fed in the form of coal.
  • the fuel has an ash content of 15.6% by weight and a moisture content of 5.6% by weight.
  • cleaned flue gas is introduced as a fluidizing gas through the grate (50) in an amount of 1527 Nm3 / h at a temperature of 150 ° C.
  • the fluidizing gas velocity is 0.2 m / s.
  • Secondary gas is introduced at a level which is approximately 1.5 m below the lower wall (62) of the solid line (56).
  • the secondary gas volume is 11454 Nm3 / h and creates a fluidizing gas velocity of 1.5 m / s above its entry point.
  • the grain fraction of less than 1 mm is fed directly into the storage container (38), whereas the coarse material is crushed to a grain size of less than 1 mm in a mill (40). 15 t / h of processed coarse grain are returned from the storage container (38) to the fluidized bed reactor (10).
  • the fluidized bed reactor (10) which is operated with a pressure loss of about 1200 mm water column - measured above rust - achieves an improvement in the heat transfer coefficient above secondary air supply of 25%.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Heterocyclic Carbon Compounds Containing A Hetero Ring Having Oxygen Or Sulfur (AREA)
  • Saccharide Compounds (AREA)
EP88201643A 1987-07-31 1988-07-30 Méthode de mise en oeuvre de processus exothermiques Expired - Lifetime EP0304111B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT88201643T ATE68578T1 (de) 1987-07-31 1988-07-30 Verfahren zur durchfuehrung exothermer prozesse.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US80424 1987-07-31
US07/080,424 US4776288A (en) 1987-07-31 1987-07-31 Method for improving solids distribution in a circulating fluidized bed system

Publications (2)

Publication Number Publication Date
EP0304111A1 true EP0304111A1 (fr) 1989-02-22
EP0304111B1 EP0304111B1 (fr) 1991-10-16

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EP88201643A Expired - Lifetime EP0304111B1 (fr) 1987-07-31 1988-07-30 Méthode de mise en oeuvre de processus exothermiques

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US (1) US4776288A (fr)
EP (1) EP0304111B1 (fr)
JP (1) JP2657526B2 (fr)
AT (1) ATE68578T1 (fr)
AU (1) AU596064B2 (fr)
CA (1) CA1281239C (fr)
DE (1) DE3865585D1 (fr)
ES (1) ES2026640T3 (fr)
ZA (1) ZA885589B (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6376248B1 (en) 1997-03-14 2002-04-23 Life Technologies, Inc. Peptide-enhanced transfections
CN102483230A (zh) * 2009-03-31 2012-05-30 阿尔斯通技术有限公司 密封罐和用于控制通过密封罐的固体流动速率的方法
US10792362B2 (en) 2014-07-15 2020-10-06 Life Technologies Corporation Compositions and methods for efficient delivery of molecules to cells

Families Citing this family (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3910271A1 (de) * 1989-03-30 1990-11-22 Saarbergwerke Ag Verfahren zum betreiben einer wirbelbettfeuerung auf kohlenbasis
US4970971A (en) * 1989-10-12 1990-11-20 Williams Robert M System of and apparatus for sanitizing waste material
JPH03213903A (ja) * 1990-01-19 1991-09-19 Nkk Corp 粒子粉砕機を備えた循環流動層燃焼装置
US5544596A (en) * 1990-02-01 1996-08-13 Abb Stal Ab Method of supplying coal and sulphur absorbent to a combustor and a power plant in which the method is applied
US5057009A (en) * 1991-01-11 1991-10-15 Wisconsin Electric Power Company Lightweight aggregate from flyash and sewage sludge
DE4200244A1 (de) * 1992-01-08 1993-07-15 Metallgesellschaft Ag Verfahren und vorrichtung zum kuehlen der heissen feststoffe eines wirbelschichtreaktors
US5218932A (en) * 1992-03-02 1993-06-15 Foster Wheeler Energy Corporation Fluidized bed reactor utilizing a baffle system and method of operating same
US5339774A (en) * 1993-07-06 1994-08-23 Foster Wheeler Energy Corporation Fluidized bed steam generation system and method of using recycled flue gases to assist in passing loopseal solids
US5500044A (en) * 1993-10-15 1996-03-19 Greengrove Corporation Process for forming aggregate; and product
US20030069173A1 (en) 1998-03-16 2003-04-10 Life Technologies, Inc. Peptide-enhanced transfections
EP1129064B1 (fr) 1998-11-12 2008-01-09 Invitrogen Corporation Reactifs de transfection
US9638418B2 (en) * 2009-05-19 2017-05-02 General Electric Technology Gmbh Oxygen fired steam generator
US20140065559A1 (en) * 2012-09-06 2014-03-06 Alstom Technology Ltd. Pressurized oxy-combustion power boiler and power plant and method of operating the same
CN103438441B (zh) * 2013-08-13 2015-09-23 东方电气集团东方锅炉股份有限公司 有效控制外置式换热器物料倒流的布风系统
CN108064329B (zh) * 2016-09-07 2020-05-08 斗山能捷斯有限责任公司 循环流化床装置
CN114229481A (zh) * 2022-02-23 2022-03-25 中国恩菲工程技术有限公司 冷却型高温粒料输送装置

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2328507A1 (fr) * 1975-10-21 1977-05-20 Battelle Development Corp Procede de traitement de matieres dans un systeme a lits fluidises
EP0082673A2 (fr) * 1981-12-17 1983-06-29 YORK-SHIPLEY, Inc. Réacteur à lit fluidifié à action rapide et procédé de l'opération dudit réacteur
US4424766A (en) * 1982-09-09 1984-01-10 Boyle Bede Alfred Hydro/pressurized fluidized bed combustor
US4434726A (en) * 1982-12-27 1984-03-06 Combustion Engineering, Inc. Fine particulate feed system for fluidized bed furnace
US4709662A (en) * 1987-01-20 1987-12-01 Riley Stoker Corporation Fluidized bed heat generator and method of operation

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4165717A (en) * 1975-09-05 1979-08-28 Metallgesellschaft Aktiengesellschaft Process for burning carbonaceous materials
DE2624302A1 (de) * 1976-05-31 1977-12-22 Metallgesellschaft Ag Verfahren zur durchfuehrung exothermer prozesse
US4244779A (en) * 1976-09-22 1981-01-13 A Ahlstrom Osakeyhtio Method of treating spent pulping liquor in a fluidized bed reactor
GB1561237A (en) * 1976-09-22 1980-02-13 Ahlstroem Oy Method of treating materials in a fluidized bed reactor
US4442797A (en) * 1983-01-24 1984-04-17 Electrodyne Research Corporation Gas and particle separation means for a steam generator circulating fluidized bed firing system
FR2563118B1 (fr) * 1984-04-20 1987-04-30 Creusot Loire Procede et installation de traitement de matiere en lit fluidise circulant
JPH0229372Y2 (fr) * 1984-09-26 1990-08-07
US4594967A (en) * 1985-03-11 1986-06-17 Foster Wheeler Energy Corporation Circulating solids fluidized bed reactor and method of operating same
EP0206066B1 (fr) * 1985-06-12 1993-03-17 Metallgesellschaft Ag Dispositif de combustion à lit fluidisé circulant

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2328507A1 (fr) * 1975-10-21 1977-05-20 Battelle Development Corp Procede de traitement de matieres dans un systeme a lits fluidises
EP0082673A2 (fr) * 1981-12-17 1983-06-29 YORK-SHIPLEY, Inc. Réacteur à lit fluidifié à action rapide et procédé de l'opération dudit réacteur
US4424766A (en) * 1982-09-09 1984-01-10 Boyle Bede Alfred Hydro/pressurized fluidized bed combustor
US4434726A (en) * 1982-12-27 1984-03-06 Combustion Engineering, Inc. Fine particulate feed system for fluidized bed furnace
US4709662A (en) * 1987-01-20 1987-12-01 Riley Stoker Corporation Fluidized bed heat generator and method of operation

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6376248B1 (en) 1997-03-14 2002-04-23 Life Technologies, Inc. Peptide-enhanced transfections
CN102483230A (zh) * 2009-03-31 2012-05-30 阿尔斯通技术有限公司 密封罐和用于控制通过密封罐的固体流动速率的方法
CN102483230B (zh) * 2009-03-31 2016-01-13 阿尔斯通技术有限公司 密封罐和用于控制通过密封罐的固体流动速率的方法
US10792362B2 (en) 2014-07-15 2020-10-06 Life Technologies Corporation Compositions and methods for efficient delivery of molecules to cells

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DE3865585D1 (de) 1991-11-21
ATE68578T1 (de) 1991-11-15
ES2026640T3 (es) 1992-05-01
CA1281239C (fr) 1991-03-12
EP0304111B1 (fr) 1991-10-16
AU2017588A (en) 1989-02-02
JPS6456134A (en) 1989-03-03
JP2657526B2 (ja) 1997-09-24
US4776288A (en) 1988-10-11
AU596064B2 (en) 1990-04-12
ZA885589B (en) 1990-03-28

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