AU6153800A - Device for thermally treating granular solid matter - Google Patents
Device for thermally treating granular solid matter Download PDFInfo
- Publication number
- AU6153800A AU6153800A AU61538/00A AU6153800A AU6153800A AU 6153800 A AU6153800 A AU 6153800A AU 61538/00 A AU61538/00 A AU 61538/00A AU 6153800 A AU6153800 A AU 6153800A AU 6153800 A AU6153800 A AU 6153800A
- Authority
- AU
- Australia
- Prior art keywords
- reactor
- solids
- gas
- solid matter
- 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
Links
- 239000007787 solid Substances 0.000 title claims abstract description 50
- 239000007789 gas Substances 0.000 claims abstract description 37
- 239000000446 fuel Substances 0.000 claims abstract description 9
- 239000000567 combustion gas Substances 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000001816 cooling Methods 0.000 claims description 7
- 238000007669 thermal treatment Methods 0.000 claims description 4
- 239000003758 nuclear fuel Substances 0.000 claims description 2
- 208000028659 discharge Diseases 0.000 claims 2
- 238000003260 vortexing Methods 0.000 abstract 1
- 230000000630 rising effect Effects 0.000 description 8
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- 239000012265 solid product Substances 0.000 description 2
- 241000272470 Circus Species 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 239000012717 electrostatic precipitator Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
Classifications
-
- 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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/14—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moving in free vortex flow apparatus
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2405—Stationary reactors without moving elements inside provoking a turbulent flow of the reactants, such as in cyclones, or having a high Reynolds-number
-
- 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
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/001—Calcining
- B01J6/004—Calcining using hot gas streams in which the material is moved
-
- 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
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/008—Pyrolysis reactions
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/44—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water
- C01F7/441—Dehydration of aluminium oxide or hydroxide, i.e. all conversions of one form into another involving a loss of water by calcination
- C01F7/444—Apparatus therefor
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
- B01J2219/00105—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling
- B01J2219/00112—Controlling the temperature by indirect heating or cooling employing heat exchange fluids part or all of the reactants being heated or cooled outside the reactor while recycling involving reactant solids
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/18—Details relating to the spatial orientation of the reactor
- B01J2219/182—Details relating to the spatial orientation of the reactor horizontal
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Treating Waste Gases (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Furnace Details (AREA)
- Processing Of Solid Wastes (AREA)
- Gasification And Melting Of Waste (AREA)
- Treatment Of Sludge (AREA)
- Cyclones (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
- Tunnel Furnaces (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
- Drying Of Solid Materials (AREA)
Abstract
The invention relates to a device for thermally treating granular solid matter for the purpose of carrying out endothermic reactions. CO2 and/or water is removed from the solid matter in a reactor by burning fuel to generate a combustion gas in the reactor, vortexing the solid matter with the combustion gases in the reactor, using hot exhaust gas from the reactor to pre-heat the solid matter and removing the solid matter from the reactor. The reactor used is an approximately cylindrical, horizontal cyclone with an approximately horizontal axis of symmetry and vortex. Fuel, solid matter and gases are supplied in an inlet zone of the reactor while a rotation vortex is formed in said inlet zone and solid matter and hot gas are removed from an outlet zone of the reactor.
Description
A 7947 Metallgesellschaft AG Bockenheimer Landstr. 73-77 D-60325 Frankfurt/Main Case No. 99 00 55 Apparatus for the Thermal Treatment of Granular Solids Description This invention relates to an apparatus for the thermal treat ment of granular solids for performing endothermic reactions, wherein CO 2 and/or water is split off from the solids, com prising a reactor to which fuel, 0 2 -containing gas and pre heated solids are supplied, wherein the fuel is burnt in the reactor to produce combustion gas with temperatures in the range from 600 to 1500 0 C, the solids in the reactor are brought in fluidizing contact with the combustion gases, hot exhaust gas from the reactor is used for preheating the sol ids, and solids are withdrawn from the reactor with tempera tures in the range from 400 to 1200*C. Apparatuses of this kind are known and described for instance in WO 97/18165 Al and GB 2 019 369, wherein alumina is pro duced from aluminum hydroxide. WO 97/18165 proposes a circu lating fluidized bed for the reactor, and in accordance with GB 2 019 369 Al the reactor is tubular with a vertical axis.
-2 It is the object underlying the invention to design the above-mentioned apparatus in a simple way, so that a rather small overall height of the plant will be sufficient. In accordance with the invention this is achieved in that the reactor constitutes an approximately cylindrical, lying cy clone with an approximately horizontal axis of symmetry and swirling, where in an inlet area of the reactor fuel, solids and gas are introduced into the reactor, and from an outlet area of the reactor disposed opposite the inlet area with a horizontal distance solids and hot exhaust gas are withdrawn. Expediently, at least one preheating cyclone is disposed be fore the reactor. In this case, preheating the solids can be performed in at least one cyclone by means of exhaust gas from the reactor, the used exhaust gas being withdrawn through a discharge line disposed in the cyclone in the man ner of a submerged tube. The discharge line designed like a submerged tube reduces the overall height and at the same time can be used for fixing the cyclone. Expediently, a cooling means is disposed subsequent to the reactor, so that solids withdrawn from the reactor are cooled in direct contact with 0 2 -containing gas and the heated 02 containing gas is introduced into the reactor, where it is required for combustion. The reactor may be used for the thermal treatment of various solids; by way of example only aluminum hydroxide should be mentioned here, which is converted to alumina. Furthermore, e.g. carbonates may be used, from which CO 2 is thermally ex pelled, in order to recover oxides. Usually, it will be en sured that at least 50 wt-% of the solids supplied to the re actor have a dwell time of at least 5 seconds in the reactor, where they are heated to the respectively required tempera ture. To achieve a prolongation of the dwell time, the hot -3 exhaust gas should expediently be withdrawn from the reactor through a discharge line which in the manner of a suspended tube protrudes into the interior of the reactor by a length T of 0.03 to 0.2 times the entire horizontal length of the re actor. This discharge line in the manner of a suspended tube provides an additional fluidization in the gas, whereby the dwell time thereof and hence also the dwell time of the sol ids in the reactor is prolonged. Embodiments of the apparatus will be explained with reference to the drawing, wherein: Fig. 1 shows a variant of the apparatus in a view, Fig. 2 shows a vertical longitudinal section through the re actor in a schematic representation, Fig. 3 shows a section along line III-III of Fig. 2 through the inlet area of the reactor as shown in Fig. 2, and Fig. 4 shows a section along line IV-IV through the outlet area of the reactor as shown in Fig. 2. The central element of the plant in accordance with Fig. 1 is the reactor 1, which approximately has the shape of a lying cylinder with a horizontal axis of symmetry and swirling. The two preheating stages include the cyclones 2 and 3 with asso ciated rising pipes 2a and 3a, to each of which solids are supplied in the base area. The solids to be treated, e.g. aluminum hydroxide, are introduced into the rising pipe 2a through line 4, in which rising pipe they are pneumatically moved into the cyclone 2 by means of hot gas from line 5. The exhaust gas leaves the cyclone 2 through line 2b, which ex tends downwards inside the cyclone 2 and opens in a gas cleaning 6. The gas cleaning may for instance be designed as wet cleaning or as electrostatic precipitator; cleaned gas is withdrawn via line 7. In practice, any number of preheating stages may be chosen.
-4 Solids preheated in the cyclone 2 leave the same through line 8 and are supplied to the base of the rising pipe 3a. Hot ex haust gas from the reactor 1, which is supplied via line 9, moves the solids to the cyclone 3, and preheated solids are supplied to the reactor 1 through line 10. Exhaust gas leaves the cyclone 3 by flowing downwards in line 5 and is supplied to the first preheating stage. If necessary, part of the sol ids coming from the cyclone 2 can be admixed to the hot sol ids of line 11, by-passing the hot area of the plant through line 8a indicated in broken lines. Through line 12, preheated, 0 2 -containing gas (e.g. air) is supplied to the reactor 1, and at the same time fuel is sup plied from line 13. To minimize the production of ash in the reactor 1, gaseous fuel, e.g. natural gas, is normally used. Usually, the combustion of the fuel with the 02-containing gas already starts at the gas inlet la of the reactor 1, and then a turbulent flow with a horizontal axis of fluidization is formed in the inlet area of the reactor 1; details will be explained below with reference to Figs. 2 to 4. The hot solid product leaves the reactor 1 through the outlet lb and is supplied to the cooling through line 11. Like pre heating, cooling can be effected in one or several stages. In the present case, two cooling stages are represented, which include the cyclones 15 and 16 and the associated rising pipes 15a and 16a. Relatively cold, 02-containing gas is supplied through line 17 to the base of the rising pipe 15a, where it moves the solid product from line 11 into the cy clone 15. The gas leaves the cyclone 15 through line 12, and the partly cooled solids reach the base of the rising pipe 16a through line 18. Relatively cold 0 2 -containing gas, e.g. ambient air, is supplied to this rising pipe 16a through line 19, and the solids are pneumatically moved into the cyclone 16. The gas then leaves the cyclone 16 through line 17, and -5 cooled solids are withdrawn via line 20. Of course, any num ber of cooling stages may be chosen. Figs. 2 to 4 show details of the reactor 1 with the gas inlet la, a solids inlet 1c, a gas outlet 9a and a solids outlet 1b. The preheated solids are supplied via line 10 and for in stance centrally supplied through the inlet ic to the inlet area of the reactor 1, where they are entrained by the com bustion gases coming from the gas inlet la. It is possible to supply the solids from line 10 wholly or partly through line 10a indicated in broken lines also through the inlet la to the reactor 1. In particular by choosing the length L and the diameter Z of the reactor 1 it should be ensured that at least 50 wt-% of the solids supplied to the reactor have a dwell time of at least 5 seconds and preferably at least 7 seconds in the re actor. The discharge line 9a is preferably designed so as to protrude into the interior of the reactor in the manner of a suspended tube preferably by a length T. This provides favor able flow conditions, which prolong the dwell times in the reactor. The length T preferably is 0.03 to 0.2 times the re actor length L. An advantageous embodiment consists in that the turbulence number, which is the ratio of axial momentum to angular momentum in consideration of the solids momentum and the quotient of inlet and outlet temperature, is larger than 1.5.
Claims (5)
1. An apparatus for the thermal treatment of granular solids for performing endothermic reactions, wherein CO 2 and/or water is split off from the solids, comprising a reactor to which fuel, 0 2 -containing gas and preheated solids are supplied, wherein the fuel is burnt in the reactor to produce combustion gas with temperatures in the range from 600 to 1500*C, the solids in the reactor are brought in fluidizing contact with the combustion gases, hot ex haust gas from the reactor is used for preheating the solids, solids are withdrawn from the reactor with tem peratures in the range from 400 to 1200 0 C and the 02 containing gas is preheated by means of the hot solids, characterized in that the reactor constitutes an approxi mately cylindrical, lying cyclone with an approximately horizontal axis of symmetry and swirling, where in an inlet area of the reactor fuel, solids and gas are intro duced into the reactor, and from an outlet area of the reactor disposed opposite the inlet area with a horizon tal distance solids and hot exhaust gas are withdrawn.
2. The apparatus as claimed in claim 1, characterized in that at least one preheating cyclone is disposed before the reactor.
3. The apparatus as claimed in claim 1 or 2, characterized in that at least one cooling means is disposed subsequent to the reactor, in which cooling means solids withdrawn from the reactor are cooled in direct contact with 02 containing gas.
4. The apparatus as claimed in claim 1 or any of the preced ing claims, characterized in that the reactor has a dis charge line for withdrawing hot exhaust gas, which dis charge line protrudes into the interior of the reactor by -7 a length T of 0.03 to 0.2 times the entire horizontal length L of the reactor.
5. The apparatus as claimed in claim 1 or any of the preced ing claims, characterized in that the solids inlet open ing of the reactor is disposed at the periphery of the reactor opposite the solids outlet.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19944778A DE19944778B4 (en) | 1999-09-17 | 1999-09-17 | Process for the thermal treatment of granular solids |
| DE19944778 | 1999-09-17 | ||
| PCT/EP2000/006174 WO2001021530A1 (en) | 1999-09-17 | 2000-07-03 | Device for thermally treating granular solid matter |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| AU6153800A true AU6153800A (en) | 2001-04-24 |
| AU778126B2 AU778126B2 (en) | 2004-11-18 |
Family
ID=7922482
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU61538/00A Ceased AU778126B2 (en) | 1999-09-17 | 2000-07-03 | Device for thermally treating granular solid matter |
Country Status (11)
| Country | Link |
|---|---|
| EP (1) | EP1212260B1 (en) |
| CN (1) | CN1197776C (en) |
| AT (1) | ATE248771T1 (en) |
| AU (1) | AU778126B2 (en) |
| BR (1) | BR0014085B1 (en) |
| CA (1) | CA2384957A1 (en) |
| DE (2) | DE19944778B4 (en) |
| EA (1) | EA004496B1 (en) |
| ES (1) | ES2204657T3 (en) |
| WO (1) | WO2001021530A1 (en) |
| ZA (1) | ZA200201890B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100406104C (en) * | 2005-01-26 | 2008-07-30 | 中国铝业股份有限公司 | Clinker dissolving out milled dust collecting method and washing tower thereof |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3752455A (en) * | 1969-08-21 | 1973-08-14 | Prerovske Strojirny Np | Arrangement for burning of pulverulent and fine grain material |
| DE2048207A1 (en) * | 1970-10-01 | 1972-04-06 | Kloeckner Humboldt Deutz Ag | Equipment for the production of alumina from alumina hydrate |
| GB2019369B (en) * | 1978-04-20 | 1982-12-01 | Smidth & Co As F L | Production of anhydrous alumina |
| RU1806309C (en) * | 1989-03-03 | 1993-03-30 | Научно-технический центр "Новатор" Приморского краевого совета ВОИР | Horizontal cyclone furnace |
| US5616303A (en) * | 1994-10-11 | 1997-04-01 | Gas Research Institute | Centrifugal bed reactor |
| DE19542309A1 (en) * | 1995-11-14 | 1997-05-15 | Metallgesellschaft Ag | Process for the production of aluminum oxide from aluminum hydroxide |
-
1999
- 1999-09-17 DE DE19944778A patent/DE19944778B4/en not_active Expired - Fee Related
-
2000
- 2000-07-03 AT AT00947911T patent/ATE248771T1/en not_active IP Right Cessation
- 2000-07-03 CA CA002384957A patent/CA2384957A1/en not_active Abandoned
- 2000-07-03 EA EA200200318A patent/EA004496B1/en not_active IP Right Cessation
- 2000-07-03 DE DE50003573T patent/DE50003573D1/en not_active Expired - Fee Related
- 2000-07-03 EP EP00947911A patent/EP1212260B1/en not_active Expired - Lifetime
- 2000-07-03 BR BRPI0014085-6A patent/BR0014085B1/en not_active IP Right Cessation
- 2000-07-03 CN CNB008144788A patent/CN1197776C/en not_active Expired - Fee Related
- 2000-07-03 ES ES00947911T patent/ES2204657T3/en not_active Expired - Lifetime
- 2000-07-03 AU AU61538/00A patent/AU778126B2/en not_active Ceased
- 2000-07-03 WO PCT/EP2000/006174 patent/WO2001021530A1/en active IP Right Grant
-
2002
- 2002-03-07 ZA ZA200201890A patent/ZA200201890B/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| BR0014085B1 (en) | 2009-01-13 |
| CA2384957A1 (en) | 2001-03-29 |
| ES2204657T3 (en) | 2004-05-01 |
| CN1379734A (en) | 2002-11-13 |
| EA004496B1 (en) | 2004-04-29 |
| AU778126B2 (en) | 2004-11-18 |
| ATE248771T1 (en) | 2003-09-15 |
| DE50003573D1 (en) | 2003-10-09 |
| EP1212260A1 (en) | 2002-06-12 |
| BR0014085A (en) | 2002-05-21 |
| WO2001021530A1 (en) | 2001-03-29 |
| ZA200201890B (en) | 2002-12-24 |
| CN1197776C (en) | 2005-04-20 |
| DE19944778A1 (en) | 2001-03-29 |
| DE19944778B4 (en) | 2004-07-08 |
| EA200200318A1 (en) | 2002-10-31 |
| EP1212260B1 (en) | 2003-09-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JPH01500251A (en) | How to reduce NOx in flue gas | |
| US4512736A (en) | Apparatus for the expansion of mineral matter, especially perlite and vermiculite | |
| CA1204274A (en) | Process of afterburning and purifying process exhaust gases | |
| US6457425B1 (en) | Method and apparatus for combustion of residual carbon in fly ash | |
| JPS61232216A (en) | Manufacture of alpha alumina in steam fluidized bed reactor | |
| JPH086097B2 (en) | Fluidized bed steam generator and method of using recycled flue gas to assist in passing loop seal solids. | |
| JP2006511420A (en) | Method and facility for producing metal oxides from metal compounds | |
| US4932862A (en) | Suspended gas reactor | |
| AU623108B2 (en) | Reactor for reducing the contents of nitrogen oxides and sulphur oxides in combustion gases | |
| AU6153800A (en) | Device for thermally treating granular solid matter | |
| US3642061A (en) | Heat exchanger | |
| US4335663A (en) | Thermal processing system | |
| GB2271517A (en) | Flue gas NOx reduction in a fluidized bed reactor | |
| GB1570276A (en) | Method and apparatus for heating particulate solids | |
| RU2219129C2 (en) | Plant for heat treatment of aluminum hydroxide | |
| JPS6326184Y2 (en) | ||
| SU1214715A1 (en) | Apparatus for heat treating of fuel | |
| JP3448591B2 (en) | Fluidized bed type firing apparatus and firing method | |
| JPS5938015B2 (en) | Calcination equipment for powder and granular raw materials | |
| SU1128081A2 (en) | Device for heat treatment of fine-grain polydispersed material | |
| SU976272A1 (en) | Device for treatment of fine-particle polydispersed material | |
| JPS587279Y2 (en) | Powder raw material calcination equipment | |
| JPS5943214B2 (en) | Method and apparatus for reducing nitrogen oxides in combustion gas | |
| JPS5664213A (en) | Method and device for fluidized bed type combustion | |
| JPS6022924A (en) | Calcining apparatus of powdered raw material |