WO1998050142A2 - Verfahren zur einstellung einer zirkulierenden wirbelschicht und verwendung des verfahrens - Google Patents
Verfahren zur einstellung einer zirkulierenden wirbelschicht und verwendung des verfahrens Download PDFInfo
- Publication number
- WO1998050142A2 WO1998050142A2 PCT/EP1998/002668 EP9802668W WO9850142A2 WO 1998050142 A2 WO1998050142 A2 WO 1998050142A2 EP 9802668 W EP9802668 W EP 9802668W WO 9850142 A2 WO9850142 A2 WO 9850142A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- fluidized bed
- cyclone
- reactor
- circulating fluidized
- mixture
- Prior art date
Links
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
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1809—Controlling processes
-
- 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
- B01J8/005—Separating solid material from the gas/liquid stream
- B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
-
- 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
- B01J8/1818—Feeding of the fluidising gas
- B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
-
- 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
- B01J8/38—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
- B01J8/384—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
- B01J8/388—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 fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/02—Oxides; Hydroxides
- C01G49/06—Ferric oxide (Fe2O3)
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/02—Oxides; Hydroxides
- C01G49/08—Ferroso-ferric oxide (Fe3O4)
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/02—Roasting processes
- C22B1/10—Roasting processes in fluidised form
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B5/00—General methods of reducing to metals
- C22B5/02—Dry methods smelting of sulfides or formation of mattes
- C22B5/12—Dry methods smelting of sulfides or formation of mattes by gases
- C22B5/14—Dry methods smelting of sulfides or formation of mattes by gases fluidised material
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/09—Reaction techniques
- Y10S423/16—Fluidization
Definitions
- the invention relates to a method for setting a circulating fluidized bed and the use of the method.
- DE-OS 39 08 972 describes an apparatus for producing powdered silicon nitride. Production takes place in a fluidized bed, nitrogen being used as the carrier gas to build up the fluidized bed.
- the procedure is known in which at least a partial stream of the clean gas discharged from the cyclone of the circulating fluidized bed is used as the carrier gas.
- the clean gas is removed from the cyclone with the aid of a rotary lobe blower and fed back to the reactor from below.
- the gases produced in the reactor contain a large amount of acidic components, primarily HCL and SO 2 . At the process temperatures, however, these acidic components quickly lead to corrosive damage to the system parts, especially the rotary lobe blower used.
- the clean gases must be cooled below the dew point before they are passed through the rotary lobe blower.
- the gases in the dew point contain larger amounts of salts in the spray at the saturation limit, which fail during compression in the rotary lobe blower, bake on and block the rotary lobe blower after a relatively short operating time.
- the invention is therefore based on the object of providing a method for setting a circulating fluidized bed in which corrosive damage to the system parts and damage caused by precipitation of salts are largely avoided.
- the object on which the invention is based is achieved by a method for setting a circulating fluidized bed, in which at least a partial stream of the clean gas discharged from the cyclone is used as a subset of the carrier gas at at least one point in the circulating fluidized bed and the clean gas used as a subset of the carrier gas the feed line into the circulating fluidized bed is mixed with 10 to 90% by weight of propellant gas, based on the amount of the partial stream of the clean gas discharged from the cyclone, in an injector mixer and the mixture is fed as carrier gas to the circulating fluidized bed.
- propellant gas for example, N 2 , air or water vapor are used as propellant.
- circulating fluidized bed is to be understood as a fluidized bed with strong movement of solids, high expansion, internal backmixing, high solids concentration at the reactor outlet with partial recycling of the solids. It essentially consists of a vertically arranged reactor, a downstream cyclone and a return line for returning solids discharged from the cyclone to the reactor.
- injector mixer is to be understood as the generally known injectors. With these injectors, one mixing partner is fed centrally into a mixing section at high speed, while the second gas stream enters the section via a remaining annular gap. Due to the high flow velocities and the speed difference at the point of entry, there is strong turbulence in the mixing section, so that the two gases can be continuously mixed.
- the mixture is supplied at least at one point in the circulating fluidized bed.
- the mixture can, for example, be fed to the reactor of the circulating fluidized bed from below. However, it is also possible to supply the mixture at one point to the return line for the solids between the cyclone and the reactor.
- a preferred embodiment of the invention is that the solids to be removed from the cyclone are at least partially passed through a U-shaped return line and fed back to the reactor and the mixture is at least partially passed into the lower part of the U-shaped return line.
- the U-shaped return line can be designed as a siphon. The initiation of at least a subset "" " .”” ,, "
- the mixture in the lower part of the U-shaped return line leads to the advantageous formation of a further fluidized bed in the lower part of the U-shaped return line.
- gases for example nitrogen
- Another advantage of this procedure is that by introducing at least a portion of the mixture into the lower part of the U-shaped return line, pressure equalization between the reactor and the cyclone can be achieved in a relatively simple manner. At the same time, the transport of the solids between the cyclone and the reactor in the return line is advantageously facilitated.
- the invention finally relates to the use of the process for the production of Fe 2 0 3 or Fe 3 0 4 . It is generally known to produce Fe 2 0 3 (red pigment) or Fe 3 0 4 (black pigment) in the circulating fluidized bed. Fe 2 0 3 is produced in an oxidizing atmosphere.
- Fe 3 0 4 is produced in a neutral or weakly reducing atmosphere.
- the raw pigments used contain a relatively large proportion of chlorine and sulfur, which is converted to HCl and SO 2 in the reactor of the circulating fluidized bed. If a partial flow of the clean gas discharged from the cyclone is used as carrier gas to build up the fluidized bed, the clean gas containing HCl and SO 2 leads to corrosive damage to the system parts.
- FIG. 1, FIG. 2). 1 shows a schematic, simplified flow diagram of the method for setting a circulating fluidized bed.
- Fig. 2 shows a schematic, simplified flow diagram of a variant of the method for setting a circulating fluidized bed.
- FIG. 1 the method for setting a circulating fluidized bed is shown in the form of a flow diagram.
- a cyclone (2) is connected downstream of the vertically arranged reactor (1) and is also connected to the reactor (1) via the return line (3).
- the entrained solids are separated in the cyclone (2) and partially removed from the system via line (4).
- Such a circulating fluidized bed is advantageously suitable for the production of Fe 2 0 3 or Fe 3 0 4 , the crude pigment, which generally contains amounts of chlorine and sulfur, being introduced into the system via line (5).
- the clean gas discharged from the cyclone (2) is discharged via line (6) and partly also removed from the system via line (11). However, a partial stream of the clean gas is fed to the injector mixer (8) via line (7).
- Nitrogen is also supplied to the injector mixer (8) as a propellant gas via line (9), which is generally to be supplied with an admission pressure of approximately 2 to 50 bar.
- the injector mixer (8) the partial amount of the clean gas used as carrier gas is mixed with the nitrogen. The mixture is then fed as the carrier gas via line (10) to the reactor (1) from below.
- FIG. 2 shows a variant of the method for setting a circulating fluidized bed in the form of a schematic, simplified flow diagram.
- the return line (3) between the cyclone (2) and the reactor (1) is U-shaped.
- the mixture discharged from the injector mixer (8) is introduced via the line (10) into the lower part of the U-shaped return line (3).
- Another fluidized bed is formed in the lower part of the U-shaped return line (3), the transport of the solids between the cyclone (2) and the reactor (1) in the return line (3) being advantageously facilitated.
- another carrier gas for example pure nitrogen, is introduced from below into the vertical reactor (1) via line (12).
Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI9809253-7A BR9809253B1 (pt) | 1997-05-07 | 1998-05-06 | processo para o ajuste de um leito fluidizado circulante e utilizaÇço do processo. |
AU77622/98A AU732310B2 (en) | 1997-05-07 | 1998-05-06 | Method of adjusting circulating fluidized bed and use of the method |
DE59801257T DE59801257D1 (de) | 1997-05-07 | 1998-05-06 | Verfahren zur einstellung einer zirkulierenden wirbelschicht und verwendung des verfahrens |
US09/423,146 US6488901B1 (en) | 1997-05-07 | 1998-05-06 | Method of adjusting a circulating fluidized bed and use of the method |
EP98925545A EP0980287B1 (de) | 1997-05-07 | 1998-05-06 | Verfahren zur einstellung einer zirkulierenden wirbelschicht und verwendung des verfahrens |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19719481A DE19719481C2 (de) | 1997-05-07 | 1997-05-07 | Verfahren zur Einstellung einer zirkulierenden Wirbelschicht |
DE19719481.8 | 1997-05-07 |
Publications (2)
Publication Number | Publication Date |
---|---|
WO1998050142A2 true WO1998050142A2 (de) | 1998-11-12 |
WO1998050142A3 WO1998050142A3 (de) | 1999-02-18 |
Family
ID=7829014
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP1998/002668 WO1998050142A2 (de) | 1997-05-07 | 1998-05-06 | Verfahren zur einstellung einer zirkulierenden wirbelschicht und verwendung des verfahrens |
Country Status (7)
Country | Link |
---|---|
US (1) | US6488901B1 (de) |
EP (1) | EP0980287B1 (de) |
AU (1) | AU732310B2 (de) |
BR (1) | BR9809253B1 (de) |
DE (2) | DE19719481C2 (de) |
WO (1) | WO1998050142A2 (de) |
ZA (1) | ZA983805B (de) |
Families Citing this family (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US6827786B2 (en) * | 2000-12-26 | 2004-12-07 | Stephen M Lord | Machine for production of granular silicon |
DE10132177A1 (de) * | 2001-07-03 | 2003-01-23 | Degussa | Verfahren zur Herstellung von Granulaten in einer zirkulierenden Wirbelschicht, Vorrichtung zur Durchführung dieses Verfahrens und nach diesem Verfahren erhaltene Granulate |
US8541051B2 (en) | 2003-08-14 | 2013-09-24 | Halliburton Energy Services, Inc. | On-the fly coating of acid-releasing degradable material onto a particulate |
US7275856B2 (en) * | 2004-09-30 | 2007-10-02 | Rohm And Haas Electronic Materials Cmp Holdings, Inc. | Apparatus for forming a polishing pad having a reduced striations |
US7714083B2 (en) * | 2006-03-08 | 2010-05-11 | Exxonmobil Chemical Patents Inc. | Recycle of hydrocarbon gases from the product tanks to a reactor through the use of ejectors |
CN101890325B (zh) * | 2009-05-20 | 2015-05-13 | 综合能源有限公司 | 细微固体颗粒回收利用装置以及包括其的流化床反应器 |
TR201111917T1 (tr) * | 2009-06-05 | 2012-05-21 | Synthesis Energy Systems, Inc. | Siklonlu ve akışkan yataklı bir reaktörden katı maddeleri geri dönüştürmek için sızdırmazlık döngüsü ve bunun kullanım yöntemi. |
WO2014032794A1 (en) * | 2012-08-29 | 2014-03-06 | Borealis Ag | Reactor assembly and method for polymerization of olefins |
US8518353B1 (en) * | 2012-10-09 | 2013-08-27 | Babcock Power Development LLC | Reduced sorbent utilization for circulating dry scrubbers |
WO2014070192A1 (en) | 2012-11-02 | 2014-05-08 | Empire Technology Development Llc | Acrylamide derivatives |
US9174871B2 (en) | 2012-11-02 | 2015-11-03 | Empire Technology Development Llc | Cement slurries having pyranose polymers |
US9238774B2 (en) | 2012-11-02 | 2016-01-19 | Empire Technology Development Llc | Soil fixation, dust suppression and water retention |
WO2014070196A1 (en) * | 2012-11-02 | 2014-05-08 | Empire Technology Development Llc | Cement slurries having pyranose polymers |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2137441A1 (en) * | 1971-05-19 | 1972-12-29 | Metallgesellschaft Ag | Fluidized bed reactors - reclaiming and recycling fines |
US4042376A (en) * | 1975-01-24 | 1977-08-16 | Stora Kopparbergs Bergslags Aktiebolag | Method for carrying out endothermic reduction processes in a circulating fluid bed and an apparatus therefor |
US4144316A (en) * | 1978-04-24 | 1979-03-13 | E. I. Du Pont De Nemours And Company | Production of chlorine and iron oxide from ferric chloride |
US4334898A (en) * | 1979-02-16 | 1982-06-15 | Swiss Aluminium Ltd. | Device for the production of solid aluminum chloride |
EP0501542A1 (de) * | 1991-02-09 | 1992-09-02 | METALLGESELLSCHAFT Aktiengesellschaft | Verfahren zum Rösten von refraktären Golderzen |
EP0543757A1 (de) * | 1991-11-19 | 1993-05-26 | Sollac | Anlage zur Eisenerzreduktion in circulierenden Wirbelschicht |
EP0549252A1 (de) * | 1991-12-23 | 1993-06-30 | BP Chemicals Limited | Verfahren zur Gasphase-Polymerisation von Alpha-Olefinen in einem Wirbelbettreaktor |
EP0685449A1 (de) * | 1994-06-02 | 1995-12-06 | The Standard Oil Company | Fliessbett-Verfahren zur Acetoxylierung von Äthylen zur Herstellung von Vinylacetat |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT287292B (de) * | 1967-08-21 | 1971-01-11 | Union Carbide Corp | Kontinuierliches Verfahren zur Herstellung von festen, teilchenförmigen Polymeren aus Olefinen |
DE3702892A1 (de) * | 1987-01-31 | 1988-08-11 | Rheinische Braunkohlenw Ag | Verfahren und einrichtung zur behandlung von koernigen feststoffen in einer wirbelschicht |
DE4210068A1 (de) * | 1992-03-27 | 1993-09-30 | Rheinische Braunkohlenw Ag | Wirbelschichtreaktor zum Verbrennen von Kohle |
-
1997
- 1997-05-07 DE DE19719481A patent/DE19719481C2/de not_active Expired - Fee Related
-
1998
- 1998-05-06 WO PCT/EP1998/002668 patent/WO1998050142A2/de active IP Right Grant
- 1998-05-06 AU AU77622/98A patent/AU732310B2/en not_active Ceased
- 1998-05-06 DE DE59801257T patent/DE59801257D1/de not_active Expired - Fee Related
- 1998-05-06 US US09/423,146 patent/US6488901B1/en not_active Expired - Fee Related
- 1998-05-06 BR BRPI9809253-7A patent/BR9809253B1/pt not_active IP Right Cessation
- 1998-05-06 ZA ZA9803805A patent/ZA983805B/xx unknown
- 1998-05-06 EP EP98925545A patent/EP0980287B1/de not_active Expired - Lifetime
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2137441A1 (en) * | 1971-05-19 | 1972-12-29 | Metallgesellschaft Ag | Fluidized bed reactors - reclaiming and recycling fines |
US4042376A (en) * | 1975-01-24 | 1977-08-16 | Stora Kopparbergs Bergslags Aktiebolag | Method for carrying out endothermic reduction processes in a circulating fluid bed and an apparatus therefor |
US4144316A (en) * | 1978-04-24 | 1979-03-13 | E. I. Du Pont De Nemours And Company | Production of chlorine and iron oxide from ferric chloride |
US4334898A (en) * | 1979-02-16 | 1982-06-15 | Swiss Aluminium Ltd. | Device for the production of solid aluminum chloride |
EP0501542A1 (de) * | 1991-02-09 | 1992-09-02 | METALLGESELLSCHAFT Aktiengesellschaft | Verfahren zum Rösten von refraktären Golderzen |
EP0543757A1 (de) * | 1991-11-19 | 1993-05-26 | Sollac | Anlage zur Eisenerzreduktion in circulierenden Wirbelschicht |
EP0549252A1 (de) * | 1991-12-23 | 1993-06-30 | BP Chemicals Limited | Verfahren zur Gasphase-Polymerisation von Alpha-Olefinen in einem Wirbelbettreaktor |
EP0685449A1 (de) * | 1994-06-02 | 1995-12-06 | The Standard Oil Company | Fliessbett-Verfahren zur Acetoxylierung von Äthylen zur Herstellung von Vinylacetat |
Also Published As
Publication number | Publication date |
---|---|
US6488901B1 (en) | 2002-12-03 |
WO1998050142A3 (de) | 1999-02-18 |
EP0980287A2 (de) | 2000-02-23 |
AU732310B2 (en) | 2001-04-12 |
DE59801257D1 (de) | 2001-09-27 |
AU7762298A (en) | 1998-11-27 |
BR9809253B1 (pt) | 2009-01-13 |
BR9809253A (pt) | 2000-10-03 |
DE19719481A1 (de) | 1998-11-12 |
DE19719481C2 (de) | 2000-09-07 |
ZA983805B (en) | 1999-11-08 |
EP0980287B1 (de) | 2001-08-22 |
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