WO2018095815A1 - Process and plant for thermal treatment in a fluidized bed reactor - Google Patents
Process and plant for thermal treatment in a fluidized bed reactor Download PDFInfo
- Publication number
- WO2018095815A1 WO2018095815A1 PCT/EP2017/079611 EP2017079611W WO2018095815A1 WO 2018095815 A1 WO2018095815 A1 WO 2018095815A1 EP 2017079611 W EP2017079611 W EP 2017079611W WO 2018095815 A1 WO2018095815 A1 WO 2018095815A1
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- WIPO (PCT)
- Prior art keywords
- gas
- reactor
- fluidized bed
- mineral
- solid
- Prior art date
Links
- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000007669 thermal treatment Methods 0.000 title claims description 10
- 239000007787 solid Substances 0.000 claims abstract description 63
- 239000002245 particle Substances 0.000 claims abstract description 43
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 38
- 239000011707 mineral Substances 0.000 claims abstract description 38
- 238000001354 calcination Methods 0.000 claims abstract description 24
- 239000000446 fuel Substances 0.000 claims abstract description 17
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 239000008247 solid mixture Substances 0.000 claims description 20
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 claims description 14
- 239000005995 Aluminium silicate Substances 0.000 claims description 9
- 235000012211 aluminium silicate Nutrition 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 claims description 6
- 238000011282 treatment Methods 0.000 claims description 6
- 239000005909 Kieselgur Substances 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000010451 perlite Substances 0.000 claims description 3
- 235000019362 perlite Nutrition 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 description 49
- 238000010438 heat treatment Methods 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 239000000463 material Substances 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000012717 electrostatic precipitator Substances 0.000 description 5
- 239000002028 Biomass Substances 0.000 description 4
- 229910052622 kaolinite Inorganic materials 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000049 pigment Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000012463 white pigment Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- PZZYQPZGQPZBDN-UHFFFAOYSA-N aluminium silicate Chemical compound O=[Al]O[Si](=O)O[Al]=O PZZYQPZGQPZBDN-UHFFFAOYSA-N 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000005469 granulation Methods 0.000 description 1
- 230000003179 granulation Effects 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 239000012719 wet electrostatic precipitator Substances 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
- 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
- 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
- B01J8/1845—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised
- B01J8/1863—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with particles moving upwards while fluidised followed by a downward movement outside the reactor and subsequently re-entering it
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/40—Compounds of aluminium
- C09C1/42—Clays
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
- B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00389—Controlling the temperature using electric heating or cooling elements
- B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00477—Controlling the temperature by thermal insulation means
- B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
Definitions
- Process and plant for thermal treatment in a fluidized bed reactor belongs to a process and the relating treatment in a fluidized bed reactor focusing on the use of biomass, which infects the feed system as well as the off-gas treatment.
- Kaolinite is a natural industrially used mineral with various applications (e.g. pigment, paper, polymer, cement, cosmetics industries, agriculture, and con- struction). Its calcination is a well-established process which is based on the thermal treatment of aluminium silicate minerals typically processed in a kiln or in hearth furnaces. As the calcination process improves the materials whiteness and hardness and its electrical properties depending on a certain exposure time at a certain temperature, it is crucial to be able to well control the temperature and residence time during the calcination process.
- the quality of the calcined kaolin is a mixture of material with very good properties with a material of lower properties in a ratio that allows for reaching the minimum requested quality.
- the residence times need to be rather long for large material amounts in order to ensure a high quality. This comes with an additional energy penalty, increasing the specific energy needed in the calcination process.
- biogas is used as an energy source which improves the process performance regarding environmental balance. Therefore, a mineral is introduced into a fluidized bed reactor in form of particles, which can be fluid- ized. Further, the biogas is injected as fuel into the fluidized bed reactor where it is burnt for generating heat to calcine the mineral. Afterwards, the calcined mineral is withdrawn from the fluidized bed in the reactor and a mixture of gas and solid particles is withdrawn from a position above the fluidized bed.
- the calcination step is the core of the process.
- Kaolin is fed to the reactor.
- the biogas is burned with air in the furnace in order to produce heat to raise the mineral particle temperature up to the desired level.
- the entrained solids are separated from the gas in a gas-solids separator (e.g. cyclone), which has an overflow and an underflow.
- the underflow contains the particles, which form the hot calcined product.
- the heat needed for the calcination is provided by e.g. burning fuel gas derived from a gasification process, or combustion of fuel.
- This option allows for the utilization of alternative fuels for the required process energy through gasification of resources which minimize the environmental footprint.
- the invention is tackling the problem of residence time and temperature control occurring to the use of biogas by using a fluidized bed technology with energy recovery.
- the residence time and the temperature can be controlled in a very narrow operating window and as such the overall efficiency of the process. It is preferred to operate this process as a continuous process. Most preferred is a steady state in the reactor.
- the mineral is granulated before being fed into the fluidized bed reactor, e.g. with addition of water).
- the available moisture in the natural resource might be sufficient for a good granulation result.
- reaction temperature lies between 800 and 1300 °C.
- Kaolin is calcined at a temperature between 1050 °C +/- 50 °C.
- the fluidized bed Compared to a rotary kiln or a hearth furnace, the fluidized bed has an excellent heat and mass transfer yielding a stable operation with a well defined and homogenous operating temperature.
- the fuel can be injected through lances and combusted without flame formation in the fluidized bed.
- kaolin as an educt, its whiteness is increased. Due to the mineral phase changes upon heating up to approximately 1 100 °C, the structure becomes denser and the hardness increases, yielding a product with improved quality suitable for the pigment industry. If the fluidized-bed process is designed well, energy efficiency can be significantly increased by recovering large fractions of sensitive heat from the off-gas and solid product by applying pre-heating and cooling stages respectively.
- the fluidized bed is a circulating fluidized bed which shows especially good heat and mass transfer rates.
- the mineral contains kaolin, diatomaceous earth and/or perlite. It is especially preferred that the used educt shows at least one of the three named minerals with a content of at least 50 wt-%, even more preferred more than 80 wt.-%
- Kaolin granules were calcined at 1050 °C +/- 100 °C without encountering major problems during calcination tests. Especially a process dealing with kaolin process is promising.
- the retention time in the circulating fluidized bed has to be very short in comparison to other minerals.
- heat can be recovered by pre-heating the feed for by pre-heating the feed for the reactor and/or by applying a fluid-bed cooler for cooling the hot calcined product.
- Heat recovery through pre-heating is achieved by contacting the hot off-gas from the reactor in a counter-current mode with the cold raw mineral feed.
- the heat remaining in the gas stream is used for drying the feed material.
- up to three pre-heating stages can be foreseen. The two-stage pre-heating starts with a moist feed, which is conveyed into the pre-heater of the first preheating stage.
- the moisture is evaporated and the solids temperature is raised.
- the gases leaving the pre-heater enter the cyclone for separation of the entrained solids.
- the off-gas is further cleaned in an electrostatic precipitator before being vented through the stack.
- the dried solids are heated to a temperature above 500 °C further reducing fuel consumption in the calcination step.
- the second stage applies the same counter-current flow of gas and solids with cooling of the gases by preheating the solids.
- a heat transfer vessel allows for the heat exchange, while the cyclone separates the solids from the gas.
- a third pre-heating step can be applied if the moisture is not too high. By this way, even higher efficiency can be achieved by making use of the sensitive heat contained in the solids and the gas.
- the first cooling of the calcined mineral is performed in multiple cyclones downstream of the furnace (bed product discharge) allowing for pre-heating of air coming from the so called fluid-bed cooler.
- the hot solids obtained as a product directly and indirectly pre-heat the air required for fluidization and establishment of process conditions allowing for complete combustion of the fuel in the reactor.
- Final cooling of the product is accomplished by water cooling (e.g. by heating water from 35 to 55 °C) allowing for adjustment of a solids temperature below 90 °C.
- the solids are treated in a fluidized bed for a defined residence time as a thermal treatment.
- said thermal treatment is a calcining.
- the solid particles are withdrawn from the fluidized bed in the reactor through a withdrawing conduit which is arranged such that during operation it is in the area of the established fluidized bed. Further, a mixture of gas and solid particles is withdrawn from a position above the fluidized bed often called free board.
- the gas normally contains the fluidizing gas, which often contains oxygen. In most of the processes fluidizing gas is air. Particles in such a mixture often show a diameter below the average diameter of the particles in the fluidized bed, so they are transported higher than these bigger particles.
- a solid fraction (preferably containing at least 70 wt.-% of the solid particles of the gas-solid mixture withdrawn from the reactor) is obtained and at least partly in the fluidized bed reactor.
- At least two cyclones are arranged in series which ensures a better separating of the solid particles from the gas-solid mixture.
- the fresh solid particles are preheated by the gas fraction obtained in one of the cyclones, whereby, the particles come in direct or indirect contact with the gas fraction obtained in at least one cyclone. Thereby, energy efficiency of the process can be increased since the fresh particles show a higher inlet temperature entering the reactor.
- a preheating is most efficient if the preheating is performed in countercur- rents.
- a second feed for feeding fresh solid particles directly into the reactor may be foreseen. Such a second position for introducing particles is especially helpful in cases of starting the process or to stabilized operating conditions.
- said second feed is preheated.
- a gas-solid mixture is withdrawn from the reactor, preferably from a position above the fluidized bed, out of the reactor.
- Such gas-solid-mixture is passed to at least one device to separate the gas fraction from a solid fraction which comprises at least 60 wt.-% of the solid particles contained in the gas- solid mixture.
- the obtained gas fraction containing SO2 and/or SO3 is passed into a packed bed to absorb SO2 and/or SO3 and withdrawing the solution with the absorbed SO 2 and/or the absorbed SO 3 .
- At least one treatment step is situated downstream of the absorption step.
- at least one step of the further treatment is an electrostatic precipitator (ESP). So it is possible to reduce dust content of the gas stream to a minimum.
- ESP electrostatic precipitator
- the gas-solid-mixture is separated in a cyclone.
- a cyclone for the feed system into the reacto-.
- the gas fraction is passed to a postcombustion before the packed bed. So, contained H 2 S is oxidized to SO2 and/or SO3 which is absorbed in the packed bed. Thereby, it is also possible to remove H 2 S present in the initial biogas.
- Such a plant comprises a reactor wherein under operating conditions a fluidized bed is established. Further, it features a feed conduit to feed at least one mineral into the reactor, a conduit to inject biogas as fuel into the fluidized bed reactor, a conduit for withdrawing calcined mineral from the fluidized bed in the reactor and a conduit for withdrawing a mixture of gas and solid particles from a position above the fluidized bed. So, , biogas can be used in a calcining process without infecting product quality.
- Such a plant comprises a reactor featuring under operating conditions a fluid- ized bed.
- Such plant further comprises two conduits, at least one cyclone and one recirculation line.
- the first conduit is able to withdraw particles from the fluidized bed since it is positioned such that during normal operation it is in the area of the fluidized bed.
- the second conduit is able to withdraw a mixture of gas and solid particles from a position above the fluidized bed and feed the mixture into at least one cyclone through which the gas-solid mixture is guided to separate a gas fraction and a solid fraction which comprises at least 60 wt. % of the solid particles contained in the withdrawn gas-solid mixture.
- solid particles from the cyclone can be re-fed into the reactor, especially in a position where the fluidized bed is established under operating conditions.
- conduit is foreseen which leads fresh solid particles into the at least one cyclone.
- the plant for thermal treatment of solid particles comprising a reactor featuring under operating conditions a fluidized bed. Further, said plant shows at least one device to separate the gas fraction from a solid fraction whereby the solid fraction comprises at least 60 wt.-% of the solid particles contained in the gas-solid mixture. Moreover, the plant features a packed bed, wherein the gas fraction containing SO2 and/or SO3 is passed to absorb SO2 and/or SO3 and a conduit is withdrawing the solution with the absorbed SO2 and/or the absorbed SO 3 .
- biogas as a green energy source without any problems concerning sulphur content in the process' off-gas.
- Fig. 1 shows the principle of the invention for calcining a mineral
- Fig. 1 shows a process for calcining a mineral using fuel as a biogas as well as the new injecting system.
- Gas of desired composition is entering via conduit 1 1 through the nozzle grate 12 and fluidizes the material in the reactor 10.
- the air Before entering the nozzle grate 12, the air can be heated by an electric pre-heating system 13 to the desired temperature. Temperature is measured at various locations and data logged.
- biogas is injected as a fuel into reactor 10. Therein fuel is burned whereby the solid particles in the fluidized bed 10 are thermally treated. Solids entrained with the reactor's off-gas in a gas-solid mixture are recirculated to the fluidized bed 10a by conduit 31 and cyclone 20. The separated solid fraction containing at least 60 wt.-% of the solids contained in the withdrawn gas-solid mixture is recirculated into the reactor 10 via conduit 26. The dustladen gas leaving the cyclone 20 passes via conduit 22 through a pre- heater 23 which can be applied for pre-drying and pre-heating the feed material which is fed into via conduit 24.
- the off-gas is then passing via conduit 25 a secondary cyclone 30 for further dust separation. Further separated parts are recycled via conduit 38 into reactor 10.
- Final dedusting of the off-gas is accomplished by passing the gas via conduit 31 in a candle filter 32 from where solid particles are withdrawn via conduit 33. If required, e.g. if H 2 S or CO are in the off-gas, the gas is bypassed through or can be treated in a post combustion chamber 36 before entering the packed bed operated as a SO2 scrubber 40. After scrubbing and passing a subsequent wet electrostatic precipitator 42 for removal of scrubbing liquid droplets and SO3, the gas leaves the system via a stack 45.
- the absolute pressure inside the reactor is close to atmospheric pressure.
- a cooling screw 50 continuously discharges material via conduits 51 , 52 from reactor bed providing the actual calcined product. Via conduit 60, it is possible to add further fresh solids into the reactor 10. Also, steam can be introduced via conduit 61 and electric pre-heating system 62.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Dispersion Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Feeding, Discharge, Calcimining, Fusing, And Gas-Generation Devices (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201780071541.5A CN109982775B (en) | 2016-11-22 | 2017-11-17 | Method and apparatus for heat treatment in a fluidized bed reactor |
AU2017365247A AU2017365247B2 (en) | 2016-11-22 | 2017-11-17 | Process and plant for thermal treatment in a fluidized bed reactor |
EP17808031.3A EP3544723A1 (en) | 2016-11-22 | 2017-11-17 | Process and plant for thermal treatment in a fluidized bed reactor |
BR112019009875-5A BR112019009875B1 (en) | 2016-11-22 | 2017-11-17 | PROCESS AND PLANT FOR CALCINATION OF A MINERAL |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102016122466.9 | 2016-11-22 | ||
DE102016122466 | 2016-11-22 |
Publications (1)
Publication Number | Publication Date |
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WO2018095815A1 true WO2018095815A1 (en) | 2018-05-31 |
Family
ID=60543521
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/EP2017/079611 WO2018095815A1 (en) | 2016-11-22 | 2017-11-17 | Process and plant for thermal treatment in a fluidized bed reactor |
Country Status (4)
Country | Link |
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EP (1) | EP3544723A1 (en) |
CN (1) | CN109982775B (en) |
AU (1) | AU2017365247B2 (en) |
WO (1) | WO2018095815A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2024102480A1 (en) * | 2022-11-11 | 2024-05-16 | Carbon Engineering Ulc | Calcination of carbonate materials |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
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CN111944333B (en) * | 2020-07-31 | 2021-11-09 | 中国科学院过程工程研究所 | Continuous fluidized calcining system and method for pearlescent material |
CN111909538B (en) * | 2020-07-31 | 2021-10-19 | 中国科学院过程工程研究所 | Continuous calcining system and method for pearlescent material |
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EP0747452A2 (en) | 1995-06-09 | 1996-12-11 | Metallgesellschaft Ag | Process for preparing a meta-kaoline white pigment from kaolinite |
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WO2005019349A2 (en) | 2003-08-11 | 2005-03-03 | Imerys Kaolin, Inc. | High whiteness metakaolin and high whiteness fully calcined kaolin |
WO2009026989A1 (en) * | 2007-09-01 | 2009-03-05 | Outotec Oyj | Process and plant for the thermal treatment of granular solids |
US20090208402A1 (en) * | 2008-02-20 | 2009-08-20 | Rossi Robert A | Process and system for producing commercial quality carbon dioxide from fine particle limestone |
WO2012145802A2 (en) * | 2011-04-27 | 2012-11-01 | Calix Limited | Reactor system and method for thermally activating minerals |
Family Cites Families (3)
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BR112019009875A2 (en) | 2019-08-06 |
EP3544723A1 (en) | 2019-10-02 |
AU2017365247B2 (en) | 2019-10-31 |
AU2017365247A1 (en) | 2019-06-13 |
CN109982775B (en) | 2022-03-29 |
CN109982775A (en) | 2019-07-05 |
BR112019009875A8 (en) | 2023-05-09 |
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