Source: http://www.google.com/patents/US7854608?dq=5191154
Timestamp: 2014-03-14 01:32:07
Document Index: 381962863

Matched Legal Cases: ['Application No. 102', 'application No. 0575245', 'application No. 196', 'application No. 3822999', 'application No. 40', 'application No. 694', 'application No. 69417103']

Patent US7854608 - Method and apparatus for heat treatment in a fluidized bed - Google PatentsSearch Images Maps Play YouTube News Gmail Drive More »Sign inAdvanced Patent SearchPatentsThe present invention relates to a method for the heat treatment of fine-grained solids, in particular gypsum, in which the solids are heated to a temperature of 50 to 1000� C. in a fluidized bed reactor (1), and to a corresponding plant. To improve the energy utilization, it is proposed to introduce...http://www.google.com/patents/US7854608?utm_source=gb-gplus-sharePatent US7854608 - Method and apparatus for heat treatment in a fluidized bedAdvanced Patent SearchPublication numberUS7854608 B2Publication typeGrantApplication numberUS 10/540,436PCT numberPCT/EP2003/013982Publication dateDec 21, 2010Filing dateDec 10, 2003Priority dateDec 23, 2002Also published asCN1729046A, CN100372600C, DE10260741A1, EP1575700A1, US20060231466, WO2004056465A1Publication number10540436, 540436, PCT/2003/13982, PCT/EP/2003/013982, PCT/EP/2003/13982, PCT/EP/3/013982, PCT/EP/3/13982, PCT/EP2003/013982, PCT/EP2003/13982, PCT/EP2003013982, PCT/EP200313982, PCT/EP3/013982, PCT/EP3/13982, PCT/EP3013982, PCT/EP313982, US 7854608 B2, US 7854608B2, US-B2-7854608, US7854608 B2, US7854608B2InventorsDirk Nuber, Werner Stockhausen, Michael Str�derOriginal AssigneeOutotec OyjExport CitationBiBTeX, EndNote, RefManPatent Citations (118), Non-Patent Citations (35), Referenced by (2), Classifications (30), Legal Events (2) External Links: USPTO, USPTO Assignment, EspacenetMethod and apparatus for heat treatment in a fluidized bedUS 7854608 B2Abstract The present invention relates to a method for the heat treatment of fine-grained solids, in particular gypsum, in which the solids are heated to a temperature of 50 to 1000� C. in a fluidized bed reactor (1), and to a corresponding plant. To improve the energy utilization, it is proposed to introduce a first gas or gas mixture from below through a preferably central gas supply tube (3) into a mixing chamber (21) of the reactor (1), the gas supply tube (3) being at least partly surrounded by a stationary annular fluidized bed (2) which is fluidized by supplying fluidizing gas, and to adjust the gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed (2) such that the particle Froude numbers in the gas supply tube (3) are between 1 and 100, in the annular fluidized bed (2) between 0.02 and 2 and in the mixing chamber (21) between 0.3 and 30.
1. A method for the heat treatment of fine-grained solids wherein the solids are heated to a temperature of 150 to 1000� C. in a fluidized bed reactor, comprising introducing a first gas or gas mixture from below through a gas supply tube into a mixing chamber of the reactor located above an annular stationary fluidized bed, the stationary annular fluidized bed being fluidized by supplying fluidizing gas, wherein the gas flowing through the gas supply tube entrains solids from the fluidized bed into the mixing chamber when passing through the upper orifice region of the gas supply tube, wherein the bed height of the solids in the reactor is adjusted such that the annular fluidized bed extends beyond the upper orifice end of the gas supply tube, and adjusting the gas velocities of the first gas or gas mixture as well as of the fluidizing gas for the annular fluidized bed such that the particle Froude numbers in the gas supply tube are between 1 and 100, in the annular fluidized bed between 0.02 and 2 and in the mixing chamber between 0.3 and 30.
This application is the national phase application under 35 U.S.C. �371 of International Application No. PCT/EP2003/013982 filed on Dec. 10, 2003, entitled, �Method And Apparatus For Heat Treatment In A Fluidized Bed� which claims the benefit of German Patent Application No. 102 60 741.9 filed on Dec. 23, 2002.
TECHNICAL FIELD The present invention relates to a method for the heat treatment of fine-grained solids, in particular gypsum, in which the solids are heated to a temperature of 50 to 1000� C. in a fluidized bed reactor, and to a corresponding plant.
DESCRIPTION OF THE INVENTION Therefore, it is the object of the present invention to improve the heat and mass transfer conditions in the heat treatment of fine-grained solids.
With the method in accordance with the invention, in particular moist gypsum, such as for example REA gypsum, can be subjected to effective heat treatment, in order in particular to obtain anhydrous forms of gypsum. The method is particularly suited for producing anhydrite by calcining. The moist gypsum used has in this case a fine granulation, the grain size of at least the majority of the solids generally being less than 2 mm. A particularly effective heat treatment can be achieved in the case of a grain size of less than 0.2 mm. Further application possibilities for the method lie in the pre-heating and/or calcining of ores and mineral raw materials in an oxidizing atmosphere at temperatures up to a maximum of approximately 1000� C., if internal combustion is ruled out, and in the calcining of clay minerals at about 800� C. At temperatures up to about 750� C., the method in accordance with the invention can also be used for producing transitional hydrates or oxides from aluminium hydroxide.
The generation of the amount of heat necessary for the operation of the reactor can be effected in any way known to the expert for this purpose, for example including by internal combustion in the reactor. To be able to use the method in accordance with the invention also for pre-heating and calcining at temperatures of for example approximately 750� C., at which an internal combustion of fuel in the reactor itself is not possible, the invention proposes the use of an external combustion chamber for generating the necessary process heat and a heat transfer to the material (for example gypsum) to be treated in the reactor with the annular fluidized bed. For this purpose, the reactor is supplied via the central tube with hot gas, which is generated in the upstream combustion chamber by burning supplied gaseous, liquid and/or solid fuel, possibly with the admixture of gas containing oxygen. Depending on the necessary oxygen content, air or some other oxygen-containing gas, for example with an oxygen content of 15 to 30%, may be admixed. Of course it is also possible to generate only part of the energy demand by burning fresh fuel and to cover the remaining part by supplying hot, fuel-free exhaust gases from a downstream stage of the process, for example cooling, or other parallel processes. If the temperatures of the exhaust gases from downstream or parallel stages of the process are adequately high, just these exhaust gases can also be used for heating the reactor. This is possible in particular whenever only low reactor temperatures are required, for example for drying. In this case, it is also possible to dispense entirely with internal combustion or an upstream combustion chamber.
Depending on the process taking place in the reactor, the process temperature may lie between 50 and 1000� C. In the lower temperature range from 50� C., in particular from approximately 80� C., the annular fluidized bed reactor may also be used only for drying material. In this case, the temperatures must not exceed an upper limit value, from which the heat-treated material undergoes a chemical reaction. In a common form of the method, a temperature range between 150 and 1000� C. is used, for example in the case of calcining.
BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 shows a process diagram of a method and a plant in accordance with a first exemplary embodiment of the present invention;
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS The plant and the method for the heat treatment of solids, such as for example gypsum, are firstly described generally on the basis of FIG. 1 to explain the functional principle according to the invention.
Example Calcining of Gypsum The calcining of REA gypsum to form water-free anhydrite is described in detail below on the basis of FIG. 2, which shows a plant similar to FIG. 1. Moist gypsum is introduced into the venturi dryer 10 by means of the screw conveyor 38 with a volumetric flow of for example 42 t/h from a storage bunker 39 and suspended by exhaust gas from the cyclone 8, dried and supplied to a separator 12, formed as a cyclone, via the solids conduit 11. The exhaust gas from the cyclone 12 is passed to a bag filter 43, where it is freed completely of solids and blown out by an exhaust gas blower 44 via a stack.
The dried gypsum separated in the cyclone 12 and the bag filter 43 is passed via solids conduits 13 to a second venturi dryer 40, heated further, separated from the exhaust gas in the cyclone 8 and introduced into the fluidized bed 2 of the reactor 1 through the solids conduit 9. In the combustion chamber 26, about 36,000 Nm3/h of hot gas with a temperature of about 1,130� C. are generated and passed to the reactor 1 through the gas-stream conduit 29. The hot gas cools in the reactor 1 to about 750� C. At the same time, the gypsum introduced into the reactor, which has a grain size of less than 0.2 mm, is heated to about 750� C. and calcined to form anhydrite. The solids are transported with the exhaust gases of the reactor 1 into the return cyclone 5 (separator), separated there and largely returned through the solids return conduit 6 into the annular fluidized bed 2 of the reactor 1.
The part-stream of the amount of anhydrite product, which corresponds to the amount of gypsum introduced into the reactor 1, is supplied through the product supply conduit 15 to the rising conduit 16 belonging to the cooling cyclone 17 of the first cooling stage 35. The anhydrite is cooled in the cooling cyclone 17 to about 600� C. and passed through the solids conduit 18 to a first chamber of the fluidized bed cooler 19. The exhaust air of the cooling cyclone 17 is passed through the supply conduit 41 to the venturi dryer 40.
In the fluidized bed cooler 19, the anhydrite is cooled in stages to about 80� C. The amount of product is about 30 t/h. During the cooling of the anhydrite, the burner air (about 14,000 Nm3/h) supplied through the air conduit 23 is indirectly heated to about 450� C. in banks of heat exchangers which are formed as cooling coils 24 and are installed in the first two chambers of the fluidized bed cooler 19. This air is supplied to the combustion chamber 26 through the supply conduit 25. As fuel, about 1,300 Nm3/h of natural gas are supplied to the combustion chamber 26 through the fuel conduit 42. In addition, further combustion air (about 21,000 Nm3/h) is blown into the combustion chamber through the air supply 28. The amount of fuel and the amount of combustion air are adjusted such that a hot-gas temperature of about 1,130� C. and the desired reactor temperature of about 750� C. are reached at the outlet of the combustion chamber 26.
List of Designations 1 reactor
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Introduction to their Industrial Chemistry and Technology, London, British Sulphur Corporation, GB, 1984, pp. 168-176, XP0006085.35Vijay, "Preoxidation and Hydrogen Reduction of Ilmenite in a Fluidized Bed Reactor" XP 000632260, Metallurgical and Material Transactions B, vol. 27B, Oct. 1996, 9. 731-738.Referenced byCiting PatentFiling datePublication dateApplicantTitleUS8048380 *Jul 10, 2009Nov 1, 2011Outotec OyjProcess and plant for producing metal oxide from metal compoundsUS20110034318 *Apr 20, 2009Feb 10, 2011Outotec OyjProcess and plant for the heat treatment of fine-grained mineral solids* Cited by examinerClassifications U.S. Classification432/16, 266/172, 75/444, 148/630International ClassificationF27B15/16, F27B15/10, B01J8/24, C22B5/14, F27B15/02, B01J8/18, B01J8/00, C22B1/10, C04B11/028Cooperative ClassificationB01J8/0055, B01J8/1863, F27B15/16, B01J2208/0053, C04B11/0283, B01J2219/00006, B01J2208/00141, F27B15/10, B01J8/1836, B01J2208/00654, B01J2208/00548, F27B15/02European ClassificationB01J8/18H, C04B11/028D, F27B15/02, B01J8/00J2, B01J8/18K4Legal EventsDateCodeEventDescriptionMar 16, 2009ASAssignmentOwner name: OUTOKUMPU TECHNOLOGY OYJ, FINLANDFree format text: CHANGE OF NAME;ASSIGNOR:OUTOKUMPU TECHNOLOGY OY;REEL/FRAME:022400/0907Effective date: 20060925Owner name: OUTOTEC OYJ, FINLANDFree format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:OUTOKUMPU TECHNOLOGY OYJ;REEL/FRAME:022401/0416Effective date: 20070423Owner name: OUTOKUMPU TECHNOLOGY OYJ,FINLANDFree format text: CHANGE OF NAME;ASSIGNOR:OUTOKUMPU TECHNOLOGY OY;US-ASSIGNMENT DATABASE UPDATED:20100406;REEL/FRAME:22400/907Owner name: OUTOTEC OYJ,FINLANDFree format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:OUTOKUMPU TECHNOLOGY OYJ;US-ASSIGNMENT DATABASE UPDATED:20100406;REEL/FRAME:22401/416Feb 17, 2006ASAssignmentOwner name: OUTOKUMPU TECHNOLOGY OY, FINLANDFree format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:NUBER, DIRK;STOCKHAUSEN, WERNER;STRODER, MICHAEL;REEL/FRAME:017185/0446;SIGNING DATES FROM 20060117 TO 20060123Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:NUBER, DIRK;STOCKHAUSEN, WERNER;STRODER, MICHAEL;SIGNINGDATES FROM 20060117 TO 20060123;REEL/FRAME:017185/0446RotateOriginal ImageGoogle Home - Sitemap - USPTO Bulk Downloads - Privacy Policy - Terms of Service - About Google Patents - Send FeedbackData provided by IFI CLAIMS Patent Services©2012 Google