• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
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  • 优先权
    • 专利摘要:
    METHOD OF IMPLEMENTATION OF ENDOTEPMHHECraiX PROCESSES in a fluidized bed cavity with a decrease in the concentration of solids from the bottom up by supplying a fluidizing gas under the gas distributor of secondary air above the gas distributor, fuel meldu points of injection of the fluidizing gas and secondary air, into the bottom distribution, and the unit will be applied to the unit. from the top of the first fluidized bed, followed by separating the solid product and returning one part of it to the fluidized bed cooling and cooling, so that, in order to increase the efficiency and efficiency of the process, the solid material separated from the first fluidized bed is subjected to additional treatment by fluidization in the second fluidized bed to complete conversion at the speed of the fluidized bed gas 0.1-0.3 m / s, while the amount of solids in the zone between the point of supplying the fluidizing gas and the point of entry of the secondary air in the first fluidizing bed is maintained at 2.0-20% by volume, in the zone above the points . Introducing secondary air of 0.22% at time vscherzhki solid material in the first fluidized bed 10-30 min and in the second fluidized bed at a time, multiple time-2-10 vscherzhki in: & first fluidized bed. about it ;:
    公开号:SU1109041A3
    申请号:SU762364358
    申请日:1976-06-03
    公开日:1984-08-15
    发明作者:Ре Лотар；ШМИДТ Ханс-Вернер；Пласс Лудольф
    申请人:Металлгезельшафт Аг (Фирма)；
    IPC主号:
    专利说明:

     .
    The invention relates to a method for carrying out endothermic processes in a fluidized state with a highly loosened fluidized bed and can be used to dehydrate crystalline inorganic compounds, for example magnesium hydroxide, iron or aluminum, calcining, for example, limestone, dolomite, deoxidation of cement, splitting of sulfuric acid. magnesium sulphate (splitting in a weakly reducing atmosphere may be appropriate), to achieve high-temperature metallurgical FIR processes such as the oxidation of ilmenite, reduction with a large finite length. recovery.
    Closest to the proposed method is the implementation of endothermic processes in a fluidized bed with a decrease in the concentration of solids from the bottom up by supplying fluidizing gas under the gas distributor, secondary gas above the gas distributor, fuel between the fluidizing gas and secondary air injection points, solid material in the lower part of the first fluidized bed and removing the solid reaction product from the top of the fluidized bed, followed by separating the solid product and returning of the fluidised bed JV.
    The disadvantage of this method is the impossibility of ensuring the minimum residence time of particles in the reactor without loss of pressure in height.
    The purpose of the invention is to increase the efficiency and effectiveness of the process.
    To achieve this goal, according to the method of performing endothermic processes in a fluidized bed with a decrease in the concentration of solids from the bottom up by supplying a fluidizing gas under the gas distributor, secondary air, above the gas distributor, t-fuel between the points of injection of the fluidizing gas and secondary air, solid material into the lower part of the first fluidized bed and removal of solid reaction product from the top of the first fluidized bed
    090А12
    followed by separating the solid product and returning one part of it to the first fluidized bed and cooling the solid material separated from the first 5 fluidized bed is further processed by fluidizing the second fluidized bed to complete conversion at a flow rate of 10 fluidized gas 0.1-0.3 m / s, while the amount of solids in the zone between the point of supplying the fluidizing gas and the point of introduction of secondary air in the first pseudots. The fluidizing layer is supported by 2.020%, and in zones e secondary air injection point 0.2-2 vol.% at time vscherzhki solid material in the first fluidized bed 1020 and 30 minutes in a fluidized bed at vtorm time 2-10-fold dwell time in the first fluidized bed.
    -j Figure 1 is a diagram of a fluidized bed reactor and a receiving reactor; Fig. 2 shows the technological scheme for the implementation of the method with cooling of the exhaust gases and solid matter; Fig. 3 shows the technological scheme for the implementation of processes carried out in a reducing atmosphere.
    Figure 1 shows the fluidized bed reactor 1, in which
    5, the gas required for fluidization enters through conduit 2, and fresh or already preheated material is supplied via conduit 3. Secondary air enters through secondary
     the air line A, the fuel is supplied through the pipe 5. The solid material removed from the reactor 1 is separated in the upper zone of the receiving reactor 6 from the gas and enters the lower zone,
    5 is slightly fluidized by the eye through the pipeline 7. The controlled return of the solid matter to the pseudo-withdrawn layer reactor is carried out through the pipeline 8, and
    0 a solid material is discharged through the outlet 9. The fuel supply, if necessary, additional heating of the receiving reactor 6 occurs through the pipeline 10.
    5 Fresh solid material is supplied by the dispenser 11 (Fig. 2) to the system of exchangers for suspended material into which the waste gases are introduced.
    fluidized bed reactor 1. First, the material enters the second (in the direction of gas flow) exchanger .12, then it is carried out and due to the high velocity of the gases enters the separators 13 and 14, where it is separated from the gas and sent to the first (along the pelvis) exchanger 15. After the second the removal through the pipeline 16 and the separation from the gas in the separator 17, it enters through the pipeline 3 into the fluidized bed reactor. The gas exiting the solid particle separator 14 is fed through line 18 to a purification system (not shown).
    The ingress into the fluidized bed reactor 1, the solid material in the zone between the fluidized bed air supplied through the pipeline 2 and the secondary air supply, becomes a suspension with relatively high density. Above the entry of the secondary duct 4, the slurry density is less. The solid material removed by the gases precipitates in the receiving reactor, and as a result of the supply of gas through the pipeline 7, it is in a low vorticity state at low speed. Pipeline 8 returns part of the solid material flow to reactor 1 under control. Another part of the flow of solid material is discharged through the outlet 9 through the pipeline 19 and the cyclone 20 into the vortex cooler 21, which consists of cooling chambers 22-25 with refrigeration pipes 26 immersed in them 26. Pipeline
    19 The fluidization air accumulates in the pipe 19, is cleaned in the cyclone 20 from solids and is sent as secondary air through the pipe 4 to the reactor 1. The incoming fluidizing air is drawn through the pipes 26
    through line 2 to reactor 1. The solid material, after being subjected to indirect cooling in two water-cooled cold rooms 27 and 28, enters pipe 29.
    Another embodiment of the invention provides for the attachment of a portion of a cyclone discharge
    20 air to gas exiting the receiving reactor 6, dp using
    it, for example, for the afterburning of the reducing components. Part of the precipitated - in the separators of solid material can be sent to the contour
    the first in the direction of the gas exchanger 15 directly through the pipeline 30 to the reactor t with a fluidized bed.
    The device specially designed for recovery processes (FIG. 3) has a different vortex cooler. Unlike the refrigerator shown in Fig. 2, there is only one cooling chamber.
    The cooling coil 31 provides preheating of air sent to the reactor 1 to form a fluidized bed. For the formation of steam is provided filled with water.
    coil 32.
    When performing reduction processes in which it is necessary to prevent the secondary oxidation of the obtained product, it is possible to use a direct-cooled, directly cooled water-cooled cyclone cooler instead of a vortex cooler 21 instead of a vortex cooler.
    In another modification of the technological scheme shown in FIG. 3, cold air is supplied not through pipeline 33, as in FIG. 2, but through a separate pipeline 34.
    Example 1 (see figure 2). Drying, ka and roasting wet after filter aluminum hydroxide.
    The reaction is carried out in a reactor 1 with an internal diameter of 2.15 m.
    with a clear height of 12 m. Secondary air is supplied at 2.5 m, and fuel oil at 0.4 m above the gas distributor.
    The inner diameter of the lower part of the receiving reactor 6, which is located under the return pipe 8, is 1.6 m with a clear height of 7 m. The vortex cooler 21 has
    6 chambers, of which four (22-25) are cooled only with air, and two chambers (27 and 28) have direct water cooling.
    Dispenser 11 delivers in the exchanger 12
    wet after the filter aluminum hydroxide (12% moisture) at a speed of 18.2 t / h.  The temperature of the gas coming from the solid separator 17 is 400 ° C.  Suspene $.  Gas / solid gas enters the separators 13 and 14 at 130 ° C.  The waste gas is vented through line 18.  The solid is directed through conduit 35 to exchanger 15 with a suspended state of the material.  Here, as a result of mixing with the gas coming from the receiving reactor with a temperature of 1100 ° C, the temperature is set at 400 ° C.  Suspension with such a temperature enters through the pipeline 16 into the separator 17 and from it via the pipeline 3 into the reactor. 1 fluidized bed.  The amount of solid at this stage is 11.5 t / h, loss on ignition is 10%.  3,600 nm / h of fluidization air and 7,100 secondary are fed to the fluidized bed reactor 1 above the gas distribution bottom. of heated air in a vortex refrigerator up to 620 and 70J3 C, respectively.  At the same time, 860 kg / hr of fuel oil is supplied via pipe 5.  Two-stage combustion ensures the achievement of 1100 ° С.  The slurry density is about 250 kg / m for the zone between the gas distribution bottom and the secondary air duct 4, and about 20 kg / m higher than the secondary air duct 4.  The resulting gas velocity (for an empty reactor) is here about 5 m / s.  Bleed out of reactor 1 together with gas. Solid particles are released in the upper part of the receiving reactor 6 and accumulate in its lower part. The fluidized bed in the receiving reactor 6 is created by introducing 180 nm of unheated air.  Through the outlet 9 is released hourly. 10.2 tons of alumina oxide, with the temperature directed through conduit 19 and cyclone 20 to a vortex cooler 21, which is supplied to form a fluidized bed of 7100 nm / h of air heated to 700 ° C.  The air directed into the cooling coil 31 at a speed of 3600 is heated to 620 ° C. - In refrigeration chambers 27 and 28, in addition, there is cooling circulating. cooling water.  Alumina is discharged through line 35 at.  1 The total residence time in reactors 1 and 6 is -1.5 hours.  This time is distributed between the fluidized bed reactor 1 and the receiving reactor 6 in the ratio of 1: 3.3.  The resulting alumina has the following granulometric composition,%: More than 90 microns 12 More than 63 microns 48 More than 44 microns 75 More than 22 microns 92 Example 2 (see FIG. H).  Calcination of dolomite to CaO, MO.  The process is carried out in a reactor 1 with an internal diameter of 2 m with a clear height of 16 m.  Secondary air is supplied at around 3 m, and fuel oil at around 0.5 m above the gas distributor.  The internal diameter of the part of the receiving reactor 6 located under the return pipe 8 is 1.4 m with a clear height of 5 ,. 5 m.  Vortex cooler 21 has six chambers, of which four (22-25) are cooled only with air, and two chambers (27 and 28) have an indirect water cooling.  Each hour, the dispenser 11 delivers 24 tons of dolomite to the exchanger 12.  The temperature of the gas leaving the separator 17 solids, 500 ° C.  The gas / solid suspension, having a temperature of 200 ° C, enters the separators 13 and 14.  The waste gas is vented through conduit 18, and the solid is transported through conduit 35 to exchanger 15. Here, as a result of mixing with the gas from the receiving reactor 6 with a temperature of 950 ° C, a temperature of 500 ° C is established.  A suspension with such a temperature enters through a conduit 16 into a separator 17, from which solid matter enters via conduit 3 to a fluidized bed reactor 1.  The reactor 1 receives 4000 nm / h of air for fluidization and 9340 nm / h of secondary air, the temperature of which is 22,650 and 700 ° C as a result of heating in the vortex cooler, respectively.  At the same time, heavy fuel oil is supplied via line 5. Two-stage combustion ensures temperature  The density of the suspension is about 250 kg / m in the area between the gas distribution bottom and the secondary air duct 4 and about 20 kg / m above the secondary air duct 4. The resulting gas velocity (for an empty reactor) is about 6.9 m / s.  The solids removed from the reactor 1 together with the gas fall out in the upper part of the receiving reactor 6 and accumulate in its lower part. The fluidization in the receiving reactor 6 is provided by supplying 180 nm / h of unheated air.  When this is achieved, the air velocity is 0.15 m / s.  The average suspension density is 1000 kg / m.  Through the outlet 9 every hour 12.6 tons of calcined material with a temperature of 900 ° C are discharged. Through the gas pipeline 19 and cyclone 20 it enters the vortex cooler 21.  Fluidization in the vortex cooler 21 is provided by supplying 9340 nm / h of air heated to.  The 31,400 ni h of air passed through the coil is heated to 650 ° C.  In the refrigeration chamber 27 and 28, cooling with circulating cooling water also occurs.  The calcined material is removed through conduit 35 at.  The total exposure of the material in reactors 1 and 6 is 1 hour.  This time is divided between the fluidized bed reactor 1 and the receiving reactor 6 in a ratio of 1: 2.  Example 3  Recovery of hematite to magnetite.  For the implementation of this method, a reactor 1 with an internal diameter of 1 m is used with a height of 18 m.  Secondary air is introduced at 3.0 m.  fuel oil - at around 0.4 m above the gas distributor.  The internal diameter of the part of the receiving reactor below the return conduit 8 is 1 m, the height D of the light is 5 m.  The vortex cooler 2 has a cooling chamber 22 with an air-filled coil 31 and an air-filled coil 32 filled with water.  The dispenser 11 supplies 20 t / h of the lateritic ore with the following composition,%: Loss on ignition 8, 7 The average particle diameter is about 80 microns.  From the dispenser material enters the exchanger 12.  The gas leaving the exchanger is at a temperature.  AT.  separators 13 and 14 are fed a mixture of gas / solid with a temperature of 150 ° C.  Exhaust gas is discharged through line 18.  The solid enters through conduit 36 to exchanger 15 with the state of the material.  Here as a result of laugh. With a gas temperature of 750 ° C coming from the receiving reactor, the temperature is set at 390 ° C.  With such a temperature, the suspension enters through the pipeline 16 into the separator 17, from which solid matter enters through the pipeline 3 into the fluidized bed reactor 1.  The amount of solid here, taking into account the calcination loss, is about 18.7 t / h.  In addition to the reactor 1, 5.8 t / h of the same ores is directly added.  1223 nm / h of air for fluidization (above the distribution base plate) and 3527 nm / h of secondary air, heated in the vortex cooler 30, are also supplied there.  to 200C, as well as 421 kg / h of heavy fuel oil.  Two-stage combustion with a total excess of oxygen ensures a temperature of 750 ° C and the production of a reducing gas with the ratio CO 02 CO + COj. The flow rate of the suspension in the zone between the gas distribution bottom and the secondary air duct 4 is about 400 kg / cm, above the secondary air duct 4 - about 30 kg / m  The gas velocity here reaches (for an empty reactor) about 0.3 m / s.  The solid that is carried out with the gas from the reactor 1 falls out in the upper part of the receiving reactor 6 and accumulates in its lower part.  The fluidization bed dp is supplied to the receiving reactor 6 at 140 nm / h of unheated air.  Pipeline 10 supplies 15 kg / h of fuel oil.  Through the outlet hole 9, 17.66 tons of magnetite are drawn every hour at.  Pipeline 19 and through 1 CLAUD 20 the material enters the vortex cooler 21, where, in order to prevent re-oxidation, the magnetite is fed to a fluidized bed of 3527 nm / h of air that heats the state in the final. account up to 200 C.  The air passed through the coil 31 (1223 im / h) is also heated to 200 ° C.  The OHPA coil 32 provides additional water cooling with co-vaporization.  Magnetite is removed through conduit 35 at 200 ° C.  For both, the sinters of the subsequent sadgani. 1060 cold air is added to the reducing off-gas from the receiving reactor 6, which is heated during subsequent combustion to 750 C.  When mixing, a temperature is reached which is similar to the gas temperature in reactors 1.  and 6. .  The total exposure of the material in the reactor system 1 and 6 is 0.5 hours.  This time is distributed between the fluidized bed reactor 1 and the receiving reactor 6 in the ratio of 1: 5.  Grading . magnetite,%: Less than 100 microns 100 Less than 62.5 microns The method of the invention is implemented in a system consisting mainly of a fluidized bed reactor and a receiving reactor.  The individual stages of the entire reaction are distributed in accordance with the reaction / process requirements between the two reactors.  Consuming the greatest amount of heat in endothermic processes, the particle preheating stage takes place in a fluidized bed reactor (main reaction).  Achieving the final quality of the product, for which, as compared with the main: reaction, 5 is required. A relatively long reaction time (subsequent reaction) is due, for example, to phase conversion.  or by the Diffusion process, and a slight heat supply takes place in the receiving reactor.  Particles with a granular composition of, for example, 20-300 µm (with an average particle size d p 50) heat up and react by virtue of their high specific surface very quickly.  Therefore, in most cases, about 90% of the entire reaction is completed after the first exit from the fluidized bed reactor.  The residual reaction then proceeds more economically with greater safety of the product and apparatus in the receiving reactor.  The method according to the invention combines the possibility of intensive heat supply to a fluidized bed reactor and smooth combustion,; achieved due to the two-stage.  In this case, the two-stage combustion can be carried out in such a way that in the case almost stoichiometric combustion is obtained.  Such a form of combustion is suitable, for example, in cases where approximately the neutral atmosphere of the furnace is required for dewatering or incineration processes.  If, according to the proposed method, a recovery process is to be carried out, then the secondary air is metered in such a way as to obtain a more or less intense reducing atmosphere.  By introducing preheated air, it is possible to achieve combustion of the waste reaction gases before they enter the exchanger with the suspended layer.  The inconvenience caused by the need to be suppressed is eliminated by supplying solids separated from the gases to the receiving reactor, which returns as much solid material as is required to maintain the required density of the suspension in the pseudo-liquefied reactor and, if necessary, to prevent a significant temperature difference between the limits of the whole system are fluidized bed reactor - receiving reactor.  The mode of operation is selected so that, taking into account the supply of fresh material as a result of the return of solid material from the receiving reactor to the fluidized bed reactor, the density of the suspension in the zone between the grate and the secondary air duct corresponds to an average solid content in the reactor space in the order of 2 -20%. With a specific gravity of 1.5 kg / l, this corresponds to a slurry density of 30–300 kg / m, and with a solid weight of 5 kg / l, the density of the suspension is 100–1000 kg / m. The density of the suspension above the secondary duct should be chosen with such By calculating the volume fraction of solids in the reactor space to be O, 2-2%. At the indicated specific gravity of solids, this corresponds to a density of 3-30 kg / m and 10-100 kg / m, respectively.  Under these conditions, the pressure in a fluidized bed reactor is about 250-900 mm of water. Art.  When assessing the working conditions of the Froude and Archimedes numbers, the following ranges are obtained: 0.1 3/4.  Fr i | 100.  0.1 s Ar ct. (fr- /, where r oVy where Fr is the Froude number, Archimedes number, gas density, kg / m, density of solid particles kg / m, diameter of spherical particles, m, kinematic viscosity.  - gravitational constant, m / s.  The density of the suspension in the receiving reactor is significantly higher due to the lower velocity of the fluidizing gas, which serves only to mix solids.  To fully utilize the receiving reactor, the proportion of solids in the total volume should exceed 35%.  Taking into account the mentioned densities, this corresponds to a lower density of the suspension of 560 and 1750 kg / m.  When estimating by the numbers of Froude and Archi honey, we obtain: the range of the number of Archim yes remains the same as in the fluidized bed reactor, for the Froude number we have -V 3/4.  Fr.  e The ratio of the dimensions of the fluidized bed reactor and the receiving reactor is determined mainly by the average total storage time required to ensure the product flow of a certain quality as well as the specific heat consumption of the endothermic process.  With a predetermined slurry density in a fluidized bed reactor and with a predetermined amount of fuel per unit of time, the increase (fall) in heat demand creates the necessary reductions (increases) in the proportion of fresh solid material supplied and increases (decreases) in the return of solid material from the receiving reactor.  It is advisable to moderately solid the material in a fluidized bed reactor for 10 to 30 minutes and 2 to 10 times the holding reactor in that time.  I. When determining the average exposure in a fluidized bed reactor, the amount of solids returned from the receiving reactor is taken into account.  The average shutter speed is determined by the sum of the average slurry density in both reactors, based on the amount of product produced in 1 hour.  The choice of the required amount of air (for fluidization and secondary air), and above all the distribution mode of both gas flows and the level of secondary air supply, provide an additional possibility of controlling the process.  In another embodiment of the method, the secondary air is supplied at a level corresponding to 10-30% of the total height of the fluidized bed reactor.  The ratio of the amount of secondary air supplied to the fluidized bed reactor to the air used for fluidization is recommended to be chosen within the range of 10: 1-1: 1, 3 / 4- Fr 5-10-e. The ratio of the sizes of the fluidized bed reactor and the receiving reactor is determined mainly the average total retention time required to ensure product delivery of a certain quality, as well as the specific heat consumption of the endothermic process.  With a predetermined slurry density in a fluidized bed reactor and with a predetermined amount of fuel per unit of time, an increase (decrease) in heat demand necessitates a decrease (increase) in the proportion of fresh solid material supplied and an increase (decrease) in the return of solid material from the receiver.  It is advisable to moderately solid the material in a fluidized bed reactor for 10-30 minutes and 2-10 times the amount in the receiving reactor.  In determining the average discharge in a fluidized bed reactor, the amount of solids returned from the receiving reactor is taken into account.  The average content is determined by the sum of the average slurry density in both reactors, calculated on the amount of product produced per hour.  The choice of the required amount of air (for fluidization and secondary air), and above all the distribution mode of both gas flows and the level of secondary air supply, provide an additional possibility of controlling the process.  In another embodiment of the method, the secondary air is supplied at a level corresponding to 10-30% of the total height of the fluidized bed reactor.  The ratio of the amount of secondary air supplied to the fluidized-bed reactor to the air used for fluidization is recommended to be chosen in the range from 10: 1 to 1: 1.  .  Due to the insignificant return of solids from the receiving reactor (due to, for example, insignificant heat demand), on the one hand, and the need for relatively long exposures, on the other hand, it is recommended to carry out heating in the receiving reactor by directly adding fuel.  Taking into account the temperature in the entire system,. Circulation is not used to fully cover the heat demand (for example, 114 radiation loss in the receiving reactor), but only for fine control of the process.  The receiving reactor is generally only intended to provide a basic holding time for the material.  Its presence may, however, cause additional effects on the solid material or reactions occurring with the solid material.  In this connection, it is possible, for example, to use inert gas for fluidization instead of air and / or to introduce chlorine or fluorine for partial chlorination or fluorination.  To ensure high thermal efficiency of the process, it is recommended to preheat and / or dehydrate the material being processed using the waste gases of a fluidized bed reactor (the operation is recommended to be carried out in exchangers in a suspended state).  Appropriate control of the temperature of the flue gases (in particular, with a wet starting product) can be achieved by partially directly, partially indirectly (after extracting heat from the flue gases) to inject the endothermically processed material into the fluidized bed reactor.  Proper distribution of the flow can provide the temperature desired for cleaning the waste gases in the electrostatic precipitator.  Sometimes it is enough to prevent the temperature falling below m. glasses of dew.  Dp of achieving high thermal efficiency, the withdrawn solid material stream is directed for cooling into a vortex cooler, preferably consisting of a series of consecutive refrigerators.  The vortex cooler can be used to preheat the secondary air and / or - using the DNP pipe registers installed in the chambers to preheat the air creating a fluidizing layer of air in the fluidized bed reactor and / or in the receiving reactor.  For fluidization in a vortex cooler, in particular during reduction processes where it is necessary to avoid re-oxidation of the reaction product, you can apply
    instead of air, an inert gas directed to its circulation circuit through a heat exchanger, for example, a venture washer, where it is cooled and, if necessary, cleaned. To increase the cooling effect, water can be injected into a whirling refrigerator.
    The amount of air supplied to the reactors is calculated so that the velocity of the gas in the fluidized bed reactor is 5-15 m / s.
    preferably 4-10 m / s and the speed in the receiving reactor was 0.1-0.3 m / s (the indicated data refer in both cases to an empty reactor).
    The operating temperature is largely unlimited and depends on the specifics of the process being carried out. The temperature may lie in the range, the lower limit of which is determined by the temperature of fuel depreciation, and the upper is approximately.
    l;
    -h
    18
    X
    权利要求:
    Claims (1)
    [1]
    METHOD FOR IMPLEMENTING ENDOTHERMIC PROCESSES in a fluidized bed with a decrease in the concentration of solids from bottom to top by supplying a fluidizing gas under the gas distributor, secondary air above the gas distributor, fuel between the points of introduction of the fluidizing gas and secondary air, the solid material into the lower part of the first fluidized bed reaction and the upper part of the first fluidized bed, followed by separation of the solid product and returning one part of it to the fluidized bed th layer and cooling, characterized in that, in order to increase the efficiency and economy of the process, the solid material separated from the first fluidized bed is subjected to additional processing by fluidization in the second fluidized bed until it is completely converted at a flow rate of 0.1 to 0.3 m / s, while the amount of solid in the zone between the point of fluidizing gas supply § and the secondary air inlet point in the first fluidizing bed is maintained at 2.0-20 vol. Foot air about 0.22 L at a holding time of the solid material in the first fluidized bed 10-30 min and in the second fluidized bed at a time, 2-10-fold dwell time in the first fluidized bed.
    ΤΤΠ6ΌΓΤ ™ “Π3>
    1 1109041
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    同族专利:
    公开号 | 公开日
    CA1079032A|1980-06-10|
    DE2524540A1|1976-12-23|
    NL180387C|1987-02-16|
    GR60266B|1978-04-20|
    AU499771B2|1979-05-03|
    IN143800B|1978-02-04|
    JPS5920380B2|1984-05-12|
    GB1500096A|1978-02-08|
    HU177477B|1981-10-28|
    ZA762959B|1977-04-27|
    FR2313120A1|1976-12-31|
    RO72150A|1982-05-10|
    YU41291B|1987-02-28|
    IT1081079B|1985-05-16|
    JPS51147478A|1976-12-17|
    US4076796A|1978-02-28|
    NL7604519A|1976-12-07|
    DE2524540C2|1986-04-24|
    YU108676A|1982-05-31|
    AU1295176A|1977-10-20|
    BR7603522A|1977-01-04|
    FR2313120B1|1980-04-04|
    NL180387B|1986-09-16|
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    申请号 | 申请日 | 专利标题
    DE2524540A|DE2524540C2|1975-06-03|1975-06-03|Process for performing endothermic processes|
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