WO1979000009A1 - Method and apparatus for carrying out chemical and/or physical processes in a fluidized bed - Google Patents
Method and apparatus for carrying out chemical and/or physical processes in a fluidized bed Download PDFInfo
- Publication number
- WO1979000009A1 WO1979000009A1 PCT/SE1978/000007 SE7800007W WO7900009A1 WO 1979000009 A1 WO1979000009 A1 WO 1979000009A1 SE 7800007 W SE7800007 W SE 7800007W WO 7900009 A1 WO7900009 A1 WO 7900009A1
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- Prior art keywords
- medium
- lighter
- fluidizing
- heavier
- wall
- Prior art date
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Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
- B01D46/32—Particle separators, e.g. dust precipitators, using loose filtering material the material moving during filtering
- B01D46/38—Particle separators, e.g. dust precipitators, using loose filtering material the material moving during filtering as fluidised bed
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
- B01D53/10—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents
- B01D53/12—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds with dispersed adsorbents according to the "fluidised technique"
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/482—Gasifiers with stationary fluidised bed
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
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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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2220/00—Aspects relating to sorbent materials
- B01J2220/50—Aspects relating to the use of sorbent or filter aid materials
- B01J2220/56—Use in the form of a bed
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
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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
- F23C2206/00—Fluidised bed combustion
- F23C2206/10—Circulating fluidised bed
- F23C2206/101—Entrained or fast fluidised bed
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2201/00—Pretreatment
- F23G2201/40—Gasification
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2209/00—Specific waste
- F23G2209/26—Biowaste
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2900/00—Special features of, or arrangements for incinerators
- F23G2900/70—Incinerating particular products or waste
- F23G2900/7013—Incinerating oil shales
Definitions
- Fluidized beds have long been known and used, primarily within the chemical process industry. Their superiority vis-a-vis conventional solid beds is ex- plained, int. al., by simplicity in the inlet and outlet of large material flows, homogeneous temperature distribution and very good heat transfer properties which lead to the avoidance of inconveniences such as local overheating, so-called "hot spots", in exothermal reactions.
- Fluidizing is obtained in that a lighter medium, for example, gas or a fluid, is allowed to flow up through a bed of a heavier (solid or fluid) medium.
- a lighter medium for example, gas or a fluid
- the bed lies motionless, but in progressively raised flow velocities, the pressure drop increases over the bed and finally, a stage is reached at which the pressure drop exceeds the force of gravity and the heavier medium begins to move.
- the bed is then described as fluidizing, and, in particular, this type of fluidized bed is., at these flow velocities, designated "bubbling", since the lighter medium is con ⁇ veyed through the heavier medium to a certain extent in the form of bubbles.
- One example of processes which advantageously may be carried out in a fluidized bed is the gasification and combustion of solid fuels such as coal, shale, wood, straw etc.
- solid fuels such as coal, shale, wood, straw etc.
- the material When a product gas with low nitrogen content is desired, the material must be gasified with oxygen gas and water vapour in order that the requisite heat be re ⁇ leased in the reactor.
- the ash can then be finally combusted with air in another reactor.
- Another method of effecting the heat supply without oxygen gas is to circulate ash between gasification and combustion beds. This involves problems with material transport and, since the systems are often under pressure, sealing problems are great.
- OMPI an absorption step a necessary part in the total process.
- the processes which are currently in operation for solid phase gas absorption are batch processes.
- continuous processes in which an expensive or otherwise valuable absorbent is utilized, and in which the utilization in ⁇ cludes a regeneration step for the absorbent, today's industry has recourse to parallel-connected units which are sequentially coupled-in according to the working schedule: absorption, regeneration, absorption," regenera- tion and so on, this arrangement being a disadvantageous solution from the point of view of process techniques and econom .
- the object of the present invention is to produce a method and apparatus which obviate the above-described inconveniences and which, in one and the same container, permit continuous and simultaneous operation of at least two separate physical and/or chemical processes in flui ⁇ dized beds between a heavier medium, for example a solid material, and different light media, for example, gaseous media, for the different chemical and/or physical proces ⁇ ses.
- a heavier medium for example a solid material
- different light media for example, gaseous media
- the beds are disposed substantially laterally separated but with an open communication between them in an area at their lower regions.
- the heavier medium is circulated between the beds via the open communication with the assistance of substantially but the one of the fluidizing media which is supplied at the open communication and is led from the associated bed substantially separate from the other fluidizing medium or media.
- the apparatus for carrying out the different chemical and/or physical processes includes a substantial- ly elongate vertical vessel ' with an inner first wall which extends in the longitudinal direction of the vessel for dividing the interior of the vessel into two co part-
- the wall being -so arranged as to permit open com ⁇ munication between the compartments over the upper and ' lower ends of the wall.
- Separate inlets are provided for the lighter media to the compartments, substantially at the lower ends of the compartments, and separate out ⁇ lets for the lighter media from the compartments.
- inlets to and outlets from the vessel for the heavy medium are also provided.
- FIG. 1 is a diametric longitudinal section through a cylindrical apparatus according to the invention
- Fig. 2 shows a modified apparatus.
- a vertical, elongate vessel with a casing wall 1, bottom wall 2 and top wall 3, has outer and inner concent ric compartments 4 and 5 for carrying out different chemical and/or physical processes in fluidized beds bet ⁇ ween a relatively heavier medium and different relatively lighter media in the two compartments 4 and 5.
- the outer compartment 4 is substantially defined by the casing wall 1 of the vessel and an elongate inner wall 6 concentric therewith, the inner wall being, at its top, connected to the casing wall by means of an upwardly inclined wall 7 and terminates, at its bottom, a distance above a perfo ⁇ rated bottom .8 sloping from the casing wall towards the centre of the vessel.
- the perforated bottom is disposed a distance above the bottom wall 2 of the vessel.
- the inner compartment 5 is substantially defined by a cylind ⁇ rical wall 9 which is concentric with and spaced apart from the wall 6, the wall 9 extending, at the bottom, past the wall 6 and terminating a distance above the per ⁇ forated bottom 8 and also delimiting the bottom end portion of the outer compartment 4 from the level at which the
- 0MP1 wall 6 has its lower end. Thus, there is open communica ⁇ tion between the compartments 4 and 5 at their lower ends.
- the cylindrical wall 9 is mounted, in a manner which is not shown, in the vessel, for example over radial walls welded to the wall 6.
- the annular-cylindrical gap which separates the walls 6 and 9 is designated 10.
- a number of inlets 11 for the heavier medium H are disposed about the casing wall 1 and discharge in this wall a distance above the lower end of the wall 6, and an outlet passage 12 from the vessel for the heavier medium extends in alignment with the compartment 5 from the perforated bottom 8 through the bottom wall 2.
- a tube 13 of smaller diameter than the compartment 5 is vertically inserted through this passage from beneath and discharges into the vessel somewhat above the perforated bottom 8 and a distance below the bottom end of the wall 9, this tube serving for blowing in lighter medium Fl into the compartment 5.
- a separator 15 for separating heavier medium from lighter medium.
- the sepa ⁇ rator may be of any given conventional cyclone arrange ⁇ ment, preferably an inner cyclone arrangement or a guide- vane arrangement according to Swedish patent application No. 7705352-8; but this arrangement may be dispensed with in certain cases, for which reason it is illustrated but schematically.
- An outlet 16 for substantially separated lighter medium is disposed in the top wall 3.
- a number of radial conduits 17 evenly distributed throughout the circumference of the casing extend through the casing wall into the space which is defined by the per ⁇ forated bottom 8, the bottom wall of the vessel 2, the casing wall 1 and the defining wall of the passage 12.
- the conduits 17 have one or more slots 18 for discharge of a second lighter medium F2 substantially into the com ⁇ partment 4 via the perforations in the perforated bottom 8.
- An outlet 19 for .essentially lighter medium F2 is dis ⁇ posed in the upper region of the casing wall 1 beneath the inclined wall 7.
- lighter media 10 that, instead, two different lighter media may be treated with one and the same heavier medium, or that heavier medium may be treated with one lighter medium and another lighter medium may be treated with the heavier medium.
- Relatively heavier medium H is introduced, if desired,
- lighter medium Fl may be adjusted from just above the minimum fluidization limit, above bubbling and turbulent, so-called rapid fluidization (as shown on
- the heavier medium in the space 14 may be separated from the lighter medium in a known manner by overflow over the upper end of the compartment 5 via, for example, an overflow outlet, and/or by utilizing the velocity re ⁇ duction in the broadened space 14, whereas, at higher velocities, a special, previously-mentioned separator 15 may be desirable for the above-mentioned separation.
- a separator may, however, always reduce the discharge of heavier medium through the outlet 16 together with lighter medium, substantially Fl, for which reason a separator is most often to be preferred in the space 14.
- heavier medium treated in the compartment .5 falls down into the fluidized bed in the compartment 4, is flui ⁇ dized therein by means of lighter medium F2 and is trans ⁇ ferred, in the previously described manner, to the com ⁇ partment 5.
- a circulation of the heavier medium takes place between the compartments 4 and 5 via the gap 10, the. heavier medium being continuously treated in the compartments 4 and 5 by means of the lighter media Fl and F2.
- Heavier medium treated in both of the compartments is removed through the outlet 12 and fluidizing medium F2 is removed through the outlet 19.
- the column in the gap may have a volume weight which varies within the limits determined by the necessity of avoiding intermixture of the lighter media in the com ⁇ partment 4 and in the space 14. It should be observed in
- lighter medium Fl may be prevented from gaining access to the reactor compartment 4 and there mixing with the lighter medium F2 thanks to the above-mentioned partial flow of lighter medium F2 to the compartment 5, this partial flow forming a barrier between the compartments 4 and 5.
- the medium F2 removed through the outlet 19 is hereby as good as free of the maxim Fl.
- the requirement of non-mixture of the lighter media may be stricter than in the utilization of the above-described first embodi ⁇ ment.
- the embodiment of the apparatus according to Fig. 1 but illustrated in Fig. 2 may be used, the same reference numerals being used in Fig. 2 for corresponding or similar details from Fig. 1.
- the injection tube 13 for the lighter medium Fl is advanced a distance into the lower end region of the reactor compartment 5 and annular channels 20 with slots 21 are disposed concentrically with and spaced apart from each other slightly above the lower end of the wall 6 in the compartment 4.
- These channels 20, whose supply lead from outside the reactor vessel is not shown, serves for the blowing in of lighter treatment and fluidizing medium F2 into the reactor com ⁇ partment 4, whereas the conduits 17 serve, in this case, for the blowing in of lighter guide medium F3.
- the task of the guide medium F3 is, on the one hand, to guide heavier medium from the compartment 4 to the lower end of the compartment 5, and, on the other hand, to fluidize the heavier medium in the compartment 4 towards the channels 20, through which the blown-in lighter treatment medium F2 creates a fluidized bed above these channels 20 for treatment of the heavier medium, by means of the medium F2, the heavier material emanating from the com ⁇ partment 5 via the gap 10 and, if continuous supply of heavier medium is effected to the vessel, from the inlets 11. Through the spaces between the channels 20, exchange takes place of heavier material between the bed created by the medium F3 and the bed created by the medium F2.
- the guide medium F3 may be selected so as to be inert with respect both to the heavier medium and the lighter treatment media so that it will have no effect on any of these media.
- a blowing box 22 may be provided beneath the perforated bottom close to the casing wall 1 for blowing in lighter treatment medium F2 into the compartment 4.
- Examples of processes which may be carried out and which have been carried out in the method according to the invention and with the apparatus of, for example, Fig. 1, are the previously-mentioned combined combustion and gasification of fluidizable fuel, such as coal, shale and biomasses.
- the organic content in the fuel which is continually introduced through the inlets 11, may be comple ⁇ tely or partially combusted and gasified in the reactor compartment 5 with a mixture of air and water, vapour.
- the gas departing from the compartment 5 may, in this case, be a low-value fuel gas or a flue gas whose energy content may be used in a boiler outside the apparatus.
- the combustion heat developed in the compartment 5 can by the above-described transport and circulation via the gap 10,of fuel material with the material as heat carrier, heat the compartment 4 where gasification with, for examp-. le,only water vapour, may take place.
- the gas emanating from the compartment 4 by the intermediary of the outlet 19 may be prevented from entraining nitrogen from the air which is introduced into the compartment 5, by the provi ⁇ sion of the previously-mentioned partial flow from the
- Nitrogen-free gas from the outlet 19 may advantageously ⁇ e used in syntheses, for pipe-line transport etc.
- a further example of the use of the invention is the previously-mentioned .absorption or adsorption processes.
- the heavier medium may constitute the absorbent or adsorbent which is to be continuously regenerated.
- the flow for example of process gas, containing the substance which is to be absorbed or adsorbed, is introduced through the channels 20 in the compartment 4 for absorption or adsorption of this substance by heavier absorption or adsorption media, and the purified gas can be removed through the outlet 19.
- Regeneration of the heavier medium is effected in the compartment 5, in which this medium is exposed to a lighter regeneration medium which is blown in through the tube 13.
- the beds formed, by the lighter media Fl and F2 may, naturally, change place in the compartments 4 and 5.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
SE7707319A SE414373B (sv) | 1977-06-23 | 1977-06-23 | Sett och apparat for genomforande av kemiska och/eller fysikaliska processer i fluidiserad bedd |
SE7707319 | 1977-06-23 |
Publications (1)
Publication Number | Publication Date |
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WO1979000009A1 true WO1979000009A1 (en) | 1979-01-11 |
Family
ID=20331672
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/SE1978/000007 WO1979000009A1 (en) | 1977-06-23 | 1978-06-22 | Method and apparatus for carrying out chemical and/or physical processes in a fluidized bed |
Country Status (4)
Country | Link |
---|---|
EP (1) | EP0007937A1 (zh-TW) |
DE (1) | DE2856921A1 (zh-TW) |
SE (1) | SE414373B (zh-TW) |
WO (1) | WO1979000009A1 (zh-TW) |
Cited By (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0047721A2 (en) * | 1980-09-10 | 1982-03-17 | CENTRO RICERCHE FIAT S.p.A. | Fluidised bed filtering and/or heat exchange apparatus particularly for gaseous discharges from internal combustion engines and industrial plants |
JPS601285A (ja) * | 1983-06-17 | 1985-01-07 | Babcock Hitachi Kk | 石炭ガス化炉の層高レベル制御方法 |
WO1986000634A1 (fr) * | 1984-07-16 | 1986-01-30 | Cockerill Mechanical Industries, Societe Anonyme | Dispositif de gazeification de dechets |
US4691031A (en) * | 1984-06-20 | 1987-09-01 | Suciu George D | Process for preventing backmixing in a fluidized bed vessel |
WO1990009548A1 (de) * | 1989-02-16 | 1990-08-23 | Saarbergwerke Aktiengesellschaft | Verfahren und anlage zur ent- oder teilentgasung von festem brennstoff |
EP0395619A1 (fr) * | 1989-04-25 | 1990-10-31 | COCKERILL MECHANICAL INDUSTRIES Société Anonyme | Procédé de traitement et d'utilisation de produits de pyrolyse et de combustion provenant d'un gazéificateur et installation pour la mise en oeuvre de ce procédé |
EP0467441A1 (de) * | 1990-07-20 | 1992-01-22 | METALLGESELLSCHAFT Aktiengesellschaft | Verfahren zur Kühlung von heissen Prozessgasen |
WO1998051967A1 (en) * | 1997-05-09 | 1998-11-19 | Corporation De L'ecole Polytechnique | Fluidized bed process and apparatus for thermally treating solid waste |
ES2128950A1 (es) * | 1995-09-15 | 1999-05-16 | Georges Allard | Reactor de lecho fluidizado denso y procedimiento de funcionamiento de tal reactor. |
WO2017103023A1 (en) * | 2015-12-17 | 2017-06-22 | Solvay Sa | Gas extraction method using adsorbent particles, adsorber and gas extraction system |
CN115040986A (zh) * | 2022-06-09 | 2022-09-13 | 中国科学院广州能源研究所 | 一种双流化床连续式含臭有机废气治理装置及方法 |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
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FI76004B (fi) * | 1986-03-24 | 1988-05-31 | Seppo Kalervo Ruottu | Cirkulationsmassareaktor. |
DE3924723C2 (de) * | 1988-08-15 | 1994-02-10 | Reinhard Dipl Ing Eckert | Energieumwandlungseinrichtung mit einer Wirbelkammerfeuerung |
FI101133B (fi) | 1996-08-30 | 1998-04-30 | Fortum Oil Oy | Laitteisto kemiallisiin ja fysikaalisiin prosesseihin |
DE102010018219A1 (de) * | 2010-04-23 | 2011-10-27 | Uhde Gmbh | Vorrichtung und Verfahren zur thermischen Vorbehandlung von festen Einsatzstoffen in einer konzentrisch gestuften Wirbelschicht |
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FR1404349A (fr) * | 1963-08-21 | 1965-06-25 | Maschf Augsburg Nuernberg Ag | Procédé d'entretien de filtre à couche filtrante |
US3236607A (en) * | 1963-06-11 | 1966-02-22 | Exxon Research Engineering Co | Apparatus for iron ore reduction |
DE2023239A1 (de) * | 1968-12-09 | 1971-11-25 | Esso Research and Engineering Co., Linden, NJ. (V.StA.) | Verfahren zur Einhaltung der Fluidität in Fliessbettsystemen |
GB1439457A (en) * | 1972-06-22 | 1976-06-16 | Exxon Research Engineering Co | Fluidised bed apparatus and uses thereof |
DE2611191A1 (de) * | 1975-03-21 | 1976-10-07 | Stora Kopparbergs Bergslags Ab | Verfahren und vorrichtung zur umwandlung eines schwefelhaltigen kohlenstoffhaltigen materials in ein im wesentlichen schwefelfreies verbrennbares gas |
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1977
- 1977-06-23 SE SE7707319A patent/SE414373B/xx unknown
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1978
- 1978-06-22 DE DE19782856921 patent/DE2856921A1/de not_active Ceased
- 1978-06-22 WO PCT/SE1978/000007 patent/WO1979000009A1/en unknown
-
1979
- 1979-01-16 EP EP78900021A patent/EP0007937A1/en not_active Withdrawn
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US3236607A (en) * | 1963-06-11 | 1966-02-22 | Exxon Research Engineering Co | Apparatus for iron ore reduction |
FR1404349A (fr) * | 1963-08-21 | 1965-06-25 | Maschf Augsburg Nuernberg Ag | Procédé d'entretien de filtre à couche filtrante |
DE2023239A1 (de) * | 1968-12-09 | 1971-11-25 | Esso Research and Engineering Co., Linden, NJ. (V.StA.) | Verfahren zur Einhaltung der Fluidität in Fliessbettsystemen |
GB1439457A (en) * | 1972-06-22 | 1976-06-16 | Exxon Research Engineering Co | Fluidised bed apparatus and uses thereof |
DE2611191A1 (de) * | 1975-03-21 | 1976-10-07 | Stora Kopparbergs Bergslags Ab | Verfahren und vorrichtung zur umwandlung eines schwefelhaltigen kohlenstoffhaltigen materials in ein im wesentlichen schwefelfreies verbrennbares gas |
Cited By (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0047721A2 (en) * | 1980-09-10 | 1982-03-17 | CENTRO RICERCHE FIAT S.p.A. | Fluidised bed filtering and/or heat exchange apparatus particularly for gaseous discharges from internal combustion engines and industrial plants |
EP0047721A3 (en) * | 1980-09-10 | 1982-05-19 | CENTRO RICERCHE FIAT S.p.A. | Fluidised bed filtering and/or heat exchange apparatus particularly for gaseous discharges from internal combustion engines and industrial plants |
JPS601285A (ja) * | 1983-06-17 | 1985-01-07 | Babcock Hitachi Kk | 石炭ガス化炉の層高レベル制御方法 |
JPH0356275B2 (zh-TW) * | 1983-06-17 | 1991-08-27 | ||
US4691031A (en) * | 1984-06-20 | 1987-09-01 | Suciu George D | Process for preventing backmixing in a fluidized bed vessel |
US4740216A (en) * | 1984-07-16 | 1988-04-26 | Cokerill Mechanical Industries, Inc. | Device for the gasification of waste |
WO1986000634A1 (fr) * | 1984-07-16 | 1986-01-30 | Cockerill Mechanical Industries, Societe Anonyme | Dispositif de gazeification de dechets |
WO1990009548A1 (de) * | 1989-02-16 | 1990-08-23 | Saarbergwerke Aktiengesellschaft | Verfahren und anlage zur ent- oder teilentgasung von festem brennstoff |
EP0395619A1 (fr) * | 1989-04-25 | 1990-10-31 | COCKERILL MECHANICAL INDUSTRIES Société Anonyme | Procédé de traitement et d'utilisation de produits de pyrolyse et de combustion provenant d'un gazéificateur et installation pour la mise en oeuvre de ce procédé |
EP0467441A1 (de) * | 1990-07-20 | 1992-01-22 | METALLGESELLSCHAFT Aktiengesellschaft | Verfahren zur Kühlung von heissen Prozessgasen |
TR25189A (tr) * | 1990-07-20 | 1993-01-01 | Metallgesellschaft Ag | Sicak islem gazlarinin sogutma islemi |
US5205350A (en) * | 1990-07-20 | 1993-04-27 | Metallgesellschaft Ag | Process for cooling a hot process gas |
ES2128950A1 (es) * | 1995-09-15 | 1999-05-16 | Georges Allard | Reactor de lecho fluidizado denso y procedimiento de funcionamiento de tal reactor. |
WO1998051967A1 (en) * | 1997-05-09 | 1998-11-19 | Corporation De L'ecole Polytechnique | Fluidized bed process and apparatus for thermally treating solid waste |
US6119607A (en) * | 1997-05-09 | 2000-09-19 | Corporation De L'ecole Polytechnique | Granular bed process for thermally treating solid waste in a flame |
WO2017103023A1 (en) * | 2015-12-17 | 2017-06-22 | Solvay Sa | Gas extraction method using adsorbent particles, adsorber and gas extraction system |
CN115040986A (zh) * | 2022-06-09 | 2022-09-13 | 中国科学院广州能源研究所 | 一种双流化床连续式含臭有机废气治理装置及方法 |
Also Published As
Publication number | Publication date |
---|---|
DE2856921A1 (de) | 1981-11-12 |
SE414373B (sv) | 1980-07-28 |
SE7707319L (sv) | 1978-12-24 |
EP0007937A1 (en) | 1980-02-20 |
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