Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F22—STEAM GENERATION
  • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
  • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
  • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
  • F22B31/0084—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed with recirculation of separated solids or with cooling of the bed particles outside the combustion bed

Definitions

• a fluid-bed heat exchanger, fluid-bed combustion reactor systems and methods for the operation of a fluid-bed heat exchanger and a fluid-bed combustion reactor system are disclosed.
• This invention concerns novel techniques of operating fluid-bed reactors, particularly fluid-bed heat exchangers for particulate material, for combustion of fuel comprising alkali, sulphur, chloride, carbon, nitrogen or the like.
• Fluid-bed systems are used in a number of processes, wherein a good contact between solid particulate material and gas is desired. Examples are heat exchange, reactions with heterogeneous catalyst and reactions directly between solid matter and gases.
• the fluid-bed principle may briefly be explained in that the solid particulates are affected by a fluidization gas introduced from below, it being within certain con ⁇ straints possible hereby to suspend the particles within a body of par ⁇ ticulate materials and keep them suspended, even though the gas flow velocity does not need to rise to a level where single particles except for the very smallest ones would be entrained and carried away by the gas flow. Under such conditions the individual particles are freely movable, but the body of the particulate material will exhibit an upper surface, i.e. it behaves like a liquid from which the name fluid-bed. Hereby, obviously a very large area of contact between the solid parti ⁇ culates and the applied gas is achieved.
• heat transfer systems In connection with a fluid-bed reactor, particularly a fluid-bed heat exchanger for particulate material, such as e.g. the fluid-bed heat exchanger disclosed in the above EP00332360, heat transfer systems are provided which normally comprise a water preheater, also designated an economizer, an evaporator, in which the water is evaporated, and a superheater, in which steam is superheated.
• a water preheater also designated an economizer
• an evaporator in which the water is evaporated
• superheater in which steam is superheated.
• the superheater in a fluid-bed is normally arranged in a more or less oxidizing environment, as the superheater tubes are arranged within the fluid-bed heat exchanger or in the exhaust gas duct.
• the superheaters arranged in the exhaust gas duct are in contact with the flue gas containing alkali chloride and the solid particles containing alkali, chloride, sulphur and the like, and are operated at a maximum steam temperature of 430-500°C. They usually have a lifetime of 7-10 years when using an appropriate material for construction thereof.
• the superheaters which are arranged in a fluid-bed heat exchanger for particulate material which is fluidized with air or other oxidizing gas may be exposed to both an oxidizing and a reducing environment.
• the super- heaters arranged in the heat exchanger for particulate material only come into contact with the solid particles containing chloride, sulphur and alkali and evaporated gases herefrom (small amounts in relation to the flue gas) and are operated at a maximum steam temperature of approx. 540°C. They usually have a lifetime of 4-7 years when using an appropriate material for construction thereof.
• Alkali, sulphur and chloride in the fuel may give rise to amounts of alkali, sulphur and chloride in the bed material too, along with che ⁇ mical compounds depending on the process conditions (temperature and gas and solid compositions). Some of these materials may under certain cir- cumstances form deposits on "cold" surfaces and may be involved in an undesired corrosion process depending on process conditions. The problem generally relating to the corrosion of heating surfaces of heat ex ⁇ changes are discussed in an article by R.U.
• the chloride corrosion rate is depending on the metal surface temperature and has a maximum in the temperature area of 600-650°C.
• the oxygen content may vary through the particle layer depending on the amount of uncombusted carbon in the bed material led to the particulate heat exchanger.
• oxidizing conditions are prevailing along the firm surfaces and in the emulsion phase.
• oxygen-free environment on the tube surface (underneath the deposit).
• the top of the particulate heat exchanger reducing conditions may in many instances be prevailing both along the surfaces and in the emulsion phase. Underneath the deposit an oxygen-free environment may exist.
• the terms “bottom”, “top”, “up” and “down” refer to the orientation relative to the vertical direction determined by the gravitational force. However, the terms may in some instances also refer to directions determined not only by the gravitational field, but determined by a virtual gravitational field generated by e.g. a high air stream flowing in a fluidizing bed from the bottom to the top which terms may due to other forces created by material flow or air flow etc. deviate from the vertical direction.
• elevated steam parameters i.e. elevated temperature and elevated pressure in the particulate heat exchanger (and longer lifetime of the particulate heat exchanger) is crucial for the obtaining of higher conversion efficiency, and therefore there is a strong incentive for increasing the steam temperature.
• a necessity for obtaining elevated steam temperatures is that the process environment surrounding the superheater is altered so that sub- stantially no corrosion occurs in the steam temperature range of 500- 700°C.
• An object of the invention is to provide novel techniques ful ⁇ filling the above necessity and in particular for reducing deposit on and/or corrosoion of the heat transfer means, arranged in a fluid-bed reactor, particularly a fluid-bed heat exchanger for particulate material, for combustion of fuel comprising alkali, sulphur, chloride, carbon, nitrogen.
• An advantage of the invention is that substantially no deposits are produced on the superheater, and corrosion by chloride or sulphide is also reduced markedly.
• a feature of the present invention is that sintering of materials together in areas of the fluid-bed heat exchanger in which areas the fluidizing conditions are less than optimum are radically reduced as compared to conventional fluid-bed coolers.
• a fluid-bed heat exchanger of a fluid-bed combustion reactor system for establishing heat transfer from heated particulate material fluidized within said fluid-bed heat exchanger to heat transfer means contained within said fluid-bed heat exchanger and internally carrying a heat-transfer medium
• said fluid-bed heat exchanger comprising gas inlet means for the introduction of a gas for the fluidization of said particulate material by means of a non-aggressive, substantially oxygen- free gas.
• the problems relating to corrosion of the heat transfer means of the fluid- bed heat exchanger, the deposition of material on the heat transfer means of the fluid-bed heat exchanger and the sintering of materials together within the fluid bed are radically reduced or basically to any substantial extent eliminated provided the fluidization of the particulate material is established by means of a substantially oxygen- free gas as oxidation or reduction processes are consequently eliminated within the fluid-bed heat exchanger.
• heat transfer is to be construed a generic term comprising any heat transfer means such as e.g. heat transfer tubes, evaporator tubes, superheater tubes, heat-pipe tubes etc.
• fuel is to be construed a generic term comprising any combustible material such as natural gas, gasoline, coal, straw material, wood material, municipal waste material or other cellulose material, biofuels etc.
• the non-aggresive, substantially oxygen-free gas by means of which the particulate material is fluidized within the fluid-bed heat exchanger according to the first aspect of the present invention may be input to the fluid-bed heat exchanger directly through the gas inlet means in accordance with embodiments to be described below or alternatively according to a first embodiment of the fluid-bed heat exchanger according to the first aspect of the present invention be produced within the fluid-bed heat exchanger as the non-aggressive, substantially oxygen-free gas is generated through the combustion internally within the fluid-bed heat exchanger of a combustable gas input to the fluid-bed heat exchanger along with atmospheric air through the gas inlet mean.
• the combustable gas may, thus, be constituted by e.g.
• natural gas which is input to the fluid-bed heat exchanger e.g. through a bottom-part thereof through nozzles and are used for the reduction of the content of oxygen of the atmospheric air which is input along with the natural gas through the above mentioned nozzles or, alternatively, through separate air inlet nozzles by the consumption of the content of oxygen of the atmospheric air or any other input gas containing oxygen through the combustion of the natural gas.
• the non-aggressive, substantially oxygen-free gas by means of which the particulate material is fluidized within the fluid-bed heat exchanger according to the first aspect of the present invention may be generated by means of any appropriate means fulfilling the basic requirement that the gas in the present environment within the fluid-bed heat exchanger is non-aggressive and is substantially oxygen-free.
• the fluid-bed heat exchanger comprises a combustion means for producing the non- aggressive, substantially oxygen-free gas from the atmospheric air through the elimination of oxygen from the atmospheric air through the combustion of fuel within the combustion means which may be constituted by e.g. a combustion engine or gas burner.
• the gas inlet means communicates with an exhaust duct of the fluid-bed combustion reactor for producing the non-aggressive, substantially oxygen-free gas from low oxygen content exhaust gas of the fluid-bed combustion reactor.
• the requirement to the fluidizing gas of the fluid-bed heat exchanger as to providing the non-aggressive, substantially oxygen-free gas is fulfilled provided the gas is non-aggressive within the present environment and further provided the content of oxygen is less than 5% by volume, such as less than 2.5% by volume, preferably approx. 0% by volume.
• the non- aggressive, substantially oxygen-free gas is constituted by an inert gas as the gas inlet means communicates with an inert gas supply for the supply of the inert gas, which may be constituted by e.g. argon, nitrogen, carbon dioxide or the like or any combination thereof.
• the non- aggressive, substantially oxygen-free gas may be constituted by steam as the gas inlet means communicates with a steam supply for the supply of steam to the fluid-bed heat exchanger.
• the fluid-bed heat exchanger may constituted a pressurized or alternatively a non-pressurized fluid-bed heat exchanger.
• the heat transfer medium which is carried internally by the heat transfer means of the fluid-bed heat exchanger according to the first aspect of the present invention may be constituted by any appropriate heat transfer medium dependent on the specific application.
• the heat transfer medium is constituted by water or steam or alternatively an inert gas such as carbondioxyde, nitrogen or fluid or gaseous natrium or potassium, in particular provided the heat transfer means are constituted by so-called heat pipes.
• the provision of the non-aggressive, substantially oxygen-free gas is described as specific alternatives, however, the techniques according to the above described five alternative embodiments may be combined as e.g. recirculated flue gas may be used in combination with an inert gas, steam etc. for input directly into the fluid-bed heat exchanger or input to e.g. a combustion engine, a gas burner or similar oxygen consuming device or means.
• the combustion established within the fluid-bed heat exchanger or externally relative to the fluid-bed heat exchanger for the consumption of oxygen i.e. the elimination of oxygen within the fluidizing gas which is used for fluidizing the particulate material within the fluid-bed heat exchanger may constitute a catalytic or alternatively a non-catalytic combustion dependent on the specific requirements and the specific application etc.
• the overall operation of the fluid-bed heat exchanger may be established by controlling the input of the gas into the fluid-bed heat exchanger for controlling the flow of the non-aggressive, substantially oxygen-free gas produced from the gas input to the fluid- bed heat exchanger or constituted by the non-aggressive, substantially oxygen-free gas itself or, alternatively, by controlling the flow of particulate material input to the fluid-bed heat exchanger as is well known within the art per se or, further alternatively, in a combined operational mode in which the operation of the fluid-bed heat exchanger is controlled by controlling the input of the gas into the fluid-bed heat controller and also the flow or particulate material input to the fluid-bed heat exchanger.
• the fluid-bed heat exchanger according to the first aspect of the present invention may be implemented in accordance with any relevant technique such as the technique disclosed in EP patent No. 0332360 and US patent No. 5014652 to which European patent reference is made and which US patent is hereby incorporated in the present specification by reference. Consequently, the fluid-bed preferably constitutes an upwards open vessel with a generally closed bottom wall and side walls, which gas inlet means is provided at which bottom wall of which upwards open vessel, and which fluid-bed heat exchanger further comprises at least one opening in the bottom wall for the discharge of particulate material from which fluid-bed heat exchanger.
• a fluid-bed combustion reactor comprising a vertical reactor chamber including a reactor chamber lower portion, a reactor chamber upper portion and an exhaust duct at which reactor chamber upper portion for the withdrawal of exhaust gas and particulate material from which reactor chamber, and a fluid-bed heat exchanger for establishing heat transfer from particulate material transferred therefrom from which reactor chamber upper portion through which exhaust duct and fluidized within which fluid-bed heat exchanger to heat transfer means, such as tubes, contained within which fluid-bed heat exchanger and internally carrying a heat-transfer medium, which fluid-bed heat exchanger comprising gas inlet means for the introduction of a non-aggressive, substantially oxygen-free gas for the fluidization of which particulate material, so as to generate which heat transfer to which heat transfer means without causing, to any substantial extent, corrosion of which heat transfer means through oxidation or reduction processes.
• the fluid-bed combustion reactor according to the second aspect of the present invention and the fluid-bed heat exchanger according to the first aspect of the present invention preferably comprise any of the features of the fluid-bed combustion reactor and the fluid-bed heat exchanger, respectively, disclosed in the above EP patent and the above US patent.
• a third aspect of the present invention obtained by a method for the operation of a fluid-bed heat exchanger for establishing heat transfer from heated particulate material fluidized within which fluid-bed heat exchanger to heat transfer means, such as tubes, contained within which fluid-bed heat exchanger and internally carrying a heat-transfer medium, which method comprising introducing a non-aggressive, substantially oxygen-free gas into which fluid-bed heat exchanger by means of gas inlet means for the fluidization of which particulate material, so as to generate which heat transfer to which heat transfer means without causing, to any substantial extent, corrosion of which heat transfer means through oxidation or reduction processes.
• a fourth aspect of the present invention obtained by a method for the operation of a fluid-bed combustion reactor, comprising a vertical reactor chamber including a reactor chamber lower portion, a reactor chamber upper portion and an exhaust duct at which reactor chamber upper portion for the withdrawal of exhaust gas and particulate material from which reactor, and a fluid-bed heat exchanger for establishing heat transfer from particulate material transferred thereto from which reactor chamber upper portion through which exhaust duct and fluidized within which fluid-bed heat exchanger to heat transfer means, such as tubes, contained within which fluid-bed heat exchanger and internally carrying a heat-transfer medium, which method comprising introducing a non-aggressive, substantially oxygen-free gas for the fluidization of which particulate material, to generate which heat transfer to which heat transfer means without causing, to any substantial extent, corrosion of which heat transfer means through oxidation or reduction processes.
• a heat changer provided as a section of a downcomer connecting the reactor chamber lower portion with the reactor chamber upper portion of a vertical reactor chamber of a fluid-bed combustion reactor system may be operated without causing to any substantial extent the formation of deposits on the heat exchanger and corrosion of the heat exchanger.
• a fluid-bed combustion reactor system comprising a vertical reactor chamber including a reactor chamber lower portion, a reactor chamber upper portion and an exhaust duct at said reactor chamber upper portion for the withdrawal of exhaust gas and particulate material from said reactor chamber, and a heat exchanger for establishing heat transfer from particulate material transferred thereto from said reactor chamber upper portion through said exhaust duct to heat transfer means, contained within said heat exchanger and internally carrying a heat- transfer medium, said heat exchanger consituting a section of a downcomer connecting said exhaust duct of said reactor chamber upper portion with said reactor chamber lower portion for the recirculation of at least part of said particulate material withdrawn from said reactor chamber.
• the heat exchanger provided within the downcomer in accordance with the further aspect of the present invention eliminates the problem associated with conventional fluid-bed super heaters as the particulate material which is recirculated by the downcomer contains carbon which reduces any oxygen present within the exhaust gas drawn through the downcomer which oxygen might else give origin to the formation of deposits on the heat exchanger and also give origin to the corrosion of the heat exchanger.
• a method of operating a fluid-bed combustion reactor system comprising a vertical reactor chamber including a reactor chamber lower portion, a reactor chamber upper portion and an exhaust duct at said reactor chamber upper portion for the withdrawal of exhaust gas and particulate material from said reactor, and a heat exchanger for establishing heat transfer from particulate material transferred thereto from said reactor chamber upper portion through said exhaust duct to heat transfer means contained within said heat exchanger and internally carrying a heat- transfer medium, said heat exchanger being a sectional heat exchanger constituting a section of a respective downcomer, said method comprising allowing said particulate material to flow down through said downcomer.
• Fig. 1 is a vertical sectional view of a first embodiment of a fluid-bed combustion reactor system illustrating three alternative ways of introducing fluidization gas according to the invention
• Fig. 2 is a reaction diagram illustrating the process conditions in the combustion of fuels
• FIG. 3 is a schematic view of a second embodiment of a combustion reactor system illustrating the technique of fluidizing particulate material within a fluid-bed heat exchanger by means of steam
• FIG. 4 is a schematic and partly sectional view of a third embodiment of a fluid-bed combustion reactor system also constituting a pressurized fluid-bed combustion reactor system including a fluid-bed heat exchanger
• Fig. 5 is a schematic and sectional view of a further embodiment of a heat exchanger constituting a sectional fluid-bed heat exchanger similar to the fluid-bed heat exchanger disclosed in US patent No. 5273 000 to which reference is made and which is hereby incorporated in the present specification by reference, and
• Fig. 6 is a schematic and partly sectional view of a further embodiment of a fluid-bed combustion reactor system comprising a downflow heat exchanger according to the present invention.
• FIG. 1 showing a vertical section through a fluid-bed combustion reactor 10 according to a first and preferred embodiment of the invention.
• This reactor 10 comprises as shown in the figure a bottom chamber 12 defined by a wall 14 and with a top chamber 16 arranged thereabove.
• the bottom chamber 12 is at the lower end provided with a discharge opening 18 with a valve mechanism 20 to allow removal of particle matters and ash, if necessary.
• a manifold or plenum chamber 22 with nozzles for the introduction of fluidization air or fluidization gas is arranged.
• the particles will not be fludized unless other fluidization means are provided here, but the particles may slide downwards to the discharge opening 18 when the valve mechanism 20 is open.
• the reactor 10 is provided with inlet ducts 24 for the introduction of particles, which may comprise fuel, inert particles, soluble reac ⁇ tants for the binding of undesired matter etc.
• Further inlets 26 for secondary reactor air may be arranged in order to allow the maintaining of a slow fluid-bed at the bottom, while a faster fluid-bed is main ⁇ tained above the secondary air inlets.
• the operation of the fluid-bed is preferably controlled in accordance with the so-called "stage combustion technique" according to which a plurality of combustion stages are produced at different elevational levels within the fluid-bed reactor through the controlling of the concentration of oxygen to be combusted within the separate stages or sections within the fluid-bed reactor.
• a further upper inlet 28 for the introduction of particulate termed fuel, inert particle, soluble reactants for the binding of undesired matter etc. may be arranged as it may be advantageous to have the possibility of selecting between various levels of introduction of such particles.
• the fluidization nozzles are provided with air/gas from blowers, each blower being provided with means to control the air/gas flow and each designated with the reference number 30. At sufficient amount of fluidization air, solid particles will be suspended by the air/gas flow and entrained by elutriation to arrive at the top chamber, where the flow is deflected sidewards by a deflector 32.
• the top chamber 16 has a larger cross sectional area than the reactor lower portion 12 and the air/gas velocity will therefore decrease in the top chamber.
• the air/gas may flow arround the deflector 32 to enter the exhaust duct 34 for flue gas. Due to the decreasing air/gas velocity in the top chamber and due to the change of flow direction, a substantial proportion of the particulate material entrained with the gas falls down into the particulate heat exchanger 36 arranged below the top chamber in accordance with a separation or sedimentation technique.
• Particles dropped down into the particle heat exchanger 36 may move downwards herein and flow through a downcomer 50 returning the particles for reintroduction into the primary reactor 10.
• the particle heat exchanger is provided with controlable blower 30 blowing fluidization air through conduits 52 upwards through the particle heat exchanger through fluidization nozzles 54 in order to fluidize the bulk of particle in the particle heat exchanger 36.
• the upper surface of the bulk particles in the particle heat exchanger is shown in the drawings at 56.
• the particle heat exchanger 36 comprises bottom wall 58 and side walls 60.
• the particle heat exchanger is provided with coolant tubes in a serpentine pattern sectionalized into two sections, which sections being designated the evaporator tube coil (not shown in the drawings, however disclosed in EP 0332360 and US 5014652 to which EP patent reference is made and which US patent is hereby incorporated in the present invention by reference) and the superheater tube coil 62. These tube coils carry water and/or steam and flow within each of the tube coils may be controlled separately.
• bottom 58 opening 64 is provided for particle discharge.
• the opening 64 takes the particles down through a downcomer 50 from the superheater section while an opening (not shown in the drawings, however disclosed in EP 0332360 and US 5014652 to which EP patent reference is made and which US patent is hereby incorporated in the present invention by reference) carries particles down to the downcomer from the evaporator section (not shown in the drawings, however disclosed in EP 0332360 and US 5014652 to which EP patent reference is made and which US patent is hereby incorporated in the present invention by reference).
• the superheater section downcomer 50 is shown shaped as an L with a relatively tall vertical portion and a relatively short horizontal por ⁇ tion at the lower end.
• an air jet 66 con ⁇ nected to a blower 30 with a blower control facility by a conduit 52 is arranged at the downcomer lower end.
• the downcomer will be filled with particles up to a level above the coolant tube coils in the particle heat exchanger. Blowing of air/gas through the jet 66 will carry particles through the downcomer horizontal portion and into the reactor as the resistance to the air blowing is lower this way.
• the pressure in the pillar of particles within the downcomer is normally so high that these particles will not be fluidized, but rather slide down-wards slowly by gravity in proportion to the amount removed at the bottom.
• Particulate material within the fluid-bed heat exchanger 36 is fluidized by blowing of gas or air through an air plenum chamber with nozzles 70.
• the bed material contains a mixture of several of these compositions, fuel ash and the basic material which may be sand, fly ash, aluminium oxide particles etc.
• the softening/adhesive temperature of the ash in the bed material very much depends on which Na and K compounds it contains. Under oxidiz ⁇ ing conditions this temperature is essentially below the combustion temperature, bed material temperature and flue gas temperature, with which there is basis for deposits of adhesive ash on the substantially colder superheater tubes.
• Fig. 1 shows fluidized particles emulsion phase areas 72 within the particle heat exchanger 36.
• the first alternative is fluidization with recirculated flue gas, which flue gas being recirculated from exhaust gas outlet 84 through recirculation conduit 80.
• the flue gas is cooled before the fluidization gas blower 30, if necessary (not shown in the drawings, however disclosed in EP 0332360 and US 5014652 to which EP patent reference is made and which US patent is hereby incorporated in the present invention by reference) and fluidization gas 86 is introduced into the gas plenum chamber 70.
• the second alternative is introduction of fluidizing gas from the blower 30 in a gas burner 76, for producing the non-aggressive, substantially oxygen-free gas from the atmospheric air through the elimination of oxygen from the atmospheric air through the combustion of the gas which fluidizing gas is cooled by a heat exchanger 82 after which the fluidization gas 86 is introduced into the gas plenum chamber 70.
• the third alternative is introduction of fluidization gas in a combustion engine 78 for producing the non-aggressive, substantially oxygen-free gas from the atmospheric air through the elimination of oxygen from the atmospheric air through the combustion of the gas wherein the exhaust gas is cooled by a heat exchanger 82 before entering the fluidization gas blower 30.
• the fluidizing gas 86 is then introduced into the gas plenum chamber 70.
• the fluidization gas comprises an inert gas, such as argon, nitrogen, carbondioxide, or the like or any combination thereof.
• the fluidizing gas comprises steam or alternatively air, which has been pretreated as mentioned above in accordance with the first, second and/or third alternative, thereby providing pretreated air containing a small amount of oxygen.
• a second embodiment of a combustion reactor system comprising a fluid-bed combustion reactor 110' of a structure similar to the structure of the fluid-bed combustion reactor 10 described above with reference to fig. 1.
• No specific discussion of the fluid-bed combustion reactor 10' is presented, as reference is made to the above discussion of the fluid-bed combustion reactor 10 of the above described first and presently preferred embodiment of the fluid-bed combustion reactor system according to the present invention.
• the fluid-bed combustion reactor system in fig. 3 further comprises a cyclone 38' similar to the above described cyclone 38 and a convection section 90, communicating with the cyclone 38' and further communicating with a steam drum 92 in a fluid-bed combustion reactor system of a structure similar to the structure of the fluid-bed combustion reactor system described in US patent No. 5273 000 to which reference is made and which is hereby incorporated in the present specification by reference.
• a cyclone 38' similar to the above described cyclone 38 and a convection section 90, communicating with the cyclone 38' and further communicating with a steam drum 92 in a fluid-bed combustion reactor system of a structure similar to the structure of the fluid-bed combustion reactor system described in US patent No. 5273 000 to which reference is made and which is hereby incorporated in the present specification by reference.
• the fluid-bed reactor 10' comprises a particle heat exchanger 36' constituting a two-section heat exchanger.
• the two sections are designated the reference numerals 94 and 96, respectively, and are provided with individual downcomers 50 and 50', respectively, similar to the downcomer 50 of the above described particle heat exchanger 36 of the fluid-bed reactor 10.
• individual super heating surfaces 98 and 100 are provided communicating with the above described steam drum 92.
• the super heating surface 100 of the section 96 further communicates with a steam turbine 102 through an inlet 104.
• the outlet of the steam turbine 102 is designated the reference numeral 106 and communicates with a section of the convection section 90 described above.
• the steam turbine 102 powers an electric generator (not shown in the drawings) or a different type of load.
• a steam extraction 108 of the steam turbine 102 is provided serving the purpose of extracting a fluidizing gas for the sections 94 and 96 of the particle heat exchanger 36' constituting non-agressive and oxygen- free fluidizing gas.
• the steam extracted from the steam turbine 102 through the steam extraction conduct 108 is directed through two valves 116 and 118 for controlling the flow rate of steam to the sections 94 and 96, respectively, of the particle heat exchanger 36'.
• an alternative technique of fluidizing the fluid-bed heat exchanger sections 94 and 96 of the particle heat exchanger 36' is also illustrated as a conduct 114 is shown for the supply of a mixture of gas and atmospheric air to the sections 94 and 96 of the particle heat exchangers 36'.
• the mixture of gas and atmospheric air is produced by means of a compressor 115 and a mixing chamber 117, and the mixture is combusted within the sections 94 and 96 of the particle heat exchanger 36' for the production of non-aggressive, substantially oxygen-free fluidizing gases.
• the fluid-bed reactor 10' is provided with a bottom particulate material discharge outlet 12'.
• a third embodiment of a combustion reactor system according to the present invention is shown consitiuting a pressurized fluid-bed combustion reactor system including a pressurized fluid-bed heat exchanger according to the present invention.
• the pressurized fluid-bed combustion reactor system is designated the reference numeral 110 and is contained within the pressure vessel 120 and further comprises a particulate fluid-bed heat exchanger 136.
• the fluid-bed combustion reactor 110 and the particulate heat exchanger 136 are basically of structures similar to the above described structures of the first and second embodiments of the fluid-bed combustion reactor systems described above with reference to figs. 1 and 3, respetively.
• the fluid-bed combustion reactor 110 also comprises a cyclone 138, the exhaust duct of which is designated the reference numeral 140 and communicates with a gas turbine 142 through a dust filter 144.
• the gas turbine 142 powers a compressor 145 for pressurizing the pressure vessel 120 and also powers an electric generator 146.
• the outlet of the gas turbine 142 is connected to a waster heat boiler 148 including a heating surface connected to a steam turbine 150 which is also connected to the particulate heat exchanger 136 through a steam conduct 152.
• the steam turbine 150 also powers an electric generator 154 and is connected to a heating surface 156 within the circuit also including the heating surface of the waste heat boiler 148.
• the steam turbine 150 is further provided with an outlet for generating the fluidizing gas for fluidizing the fluid-bed particulate heat exchanger 136 of the fluid-bed reactor 110.
• a make-up water supply conduit 162 is also provided.
• the fluidizing gas for fluidizing the fluid-bed particulate heat exchanger 156 is conducted through a conduct 158 in which a valve 160 is provided for controlling the flow rate of the steam constituting the fludizing gas.
• the fluid-bed reactor 110 is provided with a bottom particulate material discharge outlet 112.
• a further and fourth embodiment of a fluid-bed heat exchanger according to the present invention is shown constituting a sectional fluid-bed heat exchanger similar to the fluid-bed heat exchanger disclosed in US patent No. 5273000 to which reference is made and which is hereby incorporated in the present specification by reference.
• the sectional fluid-bed heat exchanger is designated the reference numeral 236 and comprises a total of four sections 236', 236", 236'" and 236"".
• Each section is provided with a bottom fluidizing gas inlet 238', 238", 238'" and 238"", respectively, for the supply of fluidizing gas constituting steam or alternatively any other appropriate, non-aggressive, substanstially oxygen-free gas for fluidizing the particulate material supplied to the sectionzed fluid-bed heat exchanger, 36, through a particulate material inlet 240 which is provided at a right hand wall of the sectional fluid-bed heat exchanger 236.
• the particulate material supplied to the sectional fluid-bed heat exchanger 236 is caused to be shifted from the first section 236' further to the second section 236" and further to the third section 236'" and finally to the fourth section 236"" from which fourth section 236"" the particulate material is returned to the reactor chamber (not shown in the drawings) through an outlet 244 causing cooling of the particulate material by heat transferring to heat transfer media carrie through respective heating surfaces 242", 242'" and 242"" of the sections 236", 236'" and 236"", respectively.
• a further or fifth embodiment of a fluid-bed combustion reactor system is shown comprising a fluid-bed reactor 210 communicating with a cyclone 238.
• the fluid-bed reactor 210 and the cyclone 238 are basically of structures similar to the structures of the fluid-bed reactor 10 and the cyclone 38 describe above with reference to fig. 1. however, the fluid-bed reactor 210 differs from the above described fluid-bed reactor 10 in that the fluid-bed particulate heat exchanger 36 of the fluid-bed reactor system shown in fig. 1 is substituted by a sectional non-fluidized heat exchanger 250.
• the sectional, non-fludized heat exchanger 250 comprises a total of three sections 250', 250" and 250'" each including a first heating surface 252', 252" and 252'", respectively, and a second heating surface 254', 254" and 254'" included within a respective downcomer 260', 260" and 260'" of each of the sections 250', 250" and 250'", respectively.
• Each downcomer is provided with a respective particulate flow control designated the reference numerals 264', 264" and 264'", respectively.
• the fluid-bed reactor 210 is provided with a bottom particulate materal outtake 212.

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• General Engineering & Computer Science (AREA)
• Fluidized-Bed Combustion And Resonant Combustion (AREA)
• Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)

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• 1995
  • 1995-07-14 AU AU29769/95A patent/AU2976995A/en not_active Abandoned
  • 1995-07-14 WO PCT/DK1995/000308 patent/WO1996002792A2/en not_active Application Discontinuation
  • 1995-07-14 EP EP95925749A patent/EP0771402A1/de not_active Withdrawn

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