RU2183651C1 - Method and apparatus for thermal processing of small-grain fuel - Google Patents

Abstract

FIELD: thermal processing equipment and methods. SUBSTANCE: method involves drying fuel; heating by mixing fuel with gas- steam mixture in heat-exchanger-adsorber and subjecting to pyrolysis in fluidized bed reactor by solid heat-carrier to obtain semicoke directed through overflow pipeline into activator and gas-steam mixture directed into heat-exchanger- adsorber; activating semicoke in activator by activating agent obtained from burnt portion of gas-steam mixture in activator muffle; delivering first portion of activator solid phase to gas-distributing grid for creating filtering fluidized bed adapted for removal of oxygen from activating agent and for improving activation conditions; directing second portion of solid phase from activator into pyrolysis reactor as solid heat-carrier; feeding third portion of solid phase from activator into gas volume of pyrolysis reactor; discharging resultant ready product - activated carbon- from activator and burning up activation gases in activator; directing produced gas phase into drier. Method and apparatus for obtaining carbonaceous sorbents may be used in branches of industry lacking activated carbons. EFFECT: increased heat efficiency by effective utilization of obtained gas-steam mixture as fuel and recovery of secondary process heat. 5 cl, 1 dwg, 1 tbl

Description

 The invention relates to methods and plants for the thermal processing of fine-grained fuel and can be used in a number of industries that require activated carbons for technological and environmental purposes - energy, chemical, metallurgical, food, pharmaceutical and other industries.

A known method of thermal processing of solid fuel, including drying and grinding of fuel, heating it with a solid heat carrier in a pyrolysis reactor to obtain a semi-coke and steam-gas mixture at 600-650 ^o C, feeding the semi-coke into the furnace and heating it, burning the combustible mass of the semi-coke in pneumatic transport mode, separating a portion of the heated char with a temperature of 850-900 ^o C from a gas phase in the first cyclone with its return as a coolant to the reactor, separating the char remaining from the gas phase in the second cyclone to a final etc. a product with the return of a portion of this product in an amount of 10-30 wt.% back to the furnace and supplying superheated water vapor in it in an amount of 5-10 wt.% of the semi-coke discharged into the furnace (RF patent 1773928, class C 10 V 49/16 12/21/90).

 A known installation for thermal processing of solid fuel, containing sequentially arranged means for drying and grinding the fuel, a cyclone for separating a drying agent, a reactor for thermal decomposition of fuel, a furnace, a cyclone for separating a heat carrier connected to the upper part of the reactor, cyclones for separating an uncoiled semi-coke, a semi-coke cooler . The furnace in the lower part is equipped with a pipe for supplying water vapor and is connected to the lower outlet of the cyclone to separate the non-trapped semi-coke (see above).

 The disadvantage of the above method and installation is that this technology can only process crushed (pulverized) fuel, for which the residue on a sieve with 200 μm cells does not exceed 30 wt.%, And with 100 μm cells - 60 wt.%. Accordingly, according to this invention, only a dusty sorbent can be obtained, which is used in a limited number of processes for the purification of liquid and gaseous media.

 In this case, the dust-like sorbent can be used only by the so-called carbohydrate method - by mixing it with the medium to be purified, followed by its precipitation from the medium to be purified, and cannot be used in sorption filters. Therefore, a dusty sorbent cannot compete with granular, the scope of which is much wider.

Another serious drawback of the indicated method and installation is the reduced yield of the finished product — activated semi-coke due to uncontrolled ratios of material streams sent to the furnace (air blast, water vapor, etc.), which leads to an increased content of free oxygen in the gas mixture supplied activation, combustion of part of the semicoke in the furnace at the stage of its activation and the formation of a large-pore sorbent structure. The relatively high temperature of 850-900 ^o C in the activation zone and the low content of water vapor in the mixture of gases injected into the furnace (5-10 wt.% Of the semi-coke introduced into the furnace) lead to the same consequences. For this reason, the yield of activated semicoke does not exceed 35% of the mass of processed fuel and the resulting semicoke has a large-pore structure with a small sorption capacity for phenols and iodine.

 There is also known a method of thermal processing of fine-grained fuel, including drying the fuel, pyrolyzing it with a solid coolant in a fluidized bed in the first reactor to obtain a semi-coke and steam-gas mixture, feeding the semi-coke into the second reactor and heating it in a fluidized bed in the presence of flue gases with removal of the finished product and return heated semi-coke to the first reactor as a solid heat carrier (Andryushchenko AI, Popov AI Fundamentals of designing energy-technological installations of power plants. M: Higher school, 1980, p. 49-53).

 The disadvantage of this technology is that it does not allow, along with other target products (resin, pyrolysis gas, etc.) to obtain a semi-coke whose properties would satisfy the requirements for carbon-containing sorbents. The semi-coke obtained by the described technology is characterized by a low sorption capacity due to the developed large-pore structure, and it contains an increased amount of small (dusty) particles less than 0.5 mm in size.

The closest known method (prototype) for the thermal processing of fine-grained fuel, in which the fuel is dried, is subjected to pyrolysis with a solid coolant in a fluidized bed in the first reactor to obtain a semi-coke and steam-gas mixture, serves semi-coke and a mixture containing flue gases and water vapor in an amount of 50-75 vol% of the mixture, with the ratio of steam to the char (1-8.): 1 to the second reactor, wherein the char is heated to 700-850 ^o C to give the final product and recycled char is heated in the first reactor as a solid Teplon rer. The oxygen content in the flue gas is 0.05-0.1 vol. % (RF patent 2074223, С 10 В 49/22, С 01 В 31/08, dated 1997).

 A known installation (according to the specified patent) for the thermal processing of fine-grained fuel, containing a first reactor for pyrolysis and a second fluidized bed reactor, interconnected by pipelines for the transfer of semi-coke and coolant. The second reactor is equipped with a muffle with a burner installed in it, separators for purification of exhaust gases with a branch pipe for their discharge and branch pipes for the output of the sorbent. The upper part of the first reactor is connected to a heat exchanger-adsorber by means of a pipeline for the removal of combined-cycle products with a supply pipe for fine-grained processed fuel installed on it. The lower part of the adsorber is connected by a pipeline with a cyclone separator to the lower part of the first reactor (see above).

 In order to prevent too intense interaction of the activated carbon-containing material with the activating vapor-gas mixture, to avoid the development of an uncontrolled activation process and excessive burning of the material with the formation of a coarse-grained sorbent structure, the oxygen content in the activating gas should be strictly limited. This is indicated in the prototype, which introduced a specific range, limiting the oxygen content in the activating gas in the range of 0.05-0.1 vol.%.

However, the real stable maintenance of the O ₂ content in gases at such a low level and within the specified strict boundaries is practically unattainable. Moreover, the prototype does not provide any means of achieving a low O ₂ content in gases and maintaining its concentration in such a narrow range.

 It is practically possible to maintain the oxygen concentration at such a low level only with the help of special means, and such a level of 0.05-0.1 vol.% Cannot be achieved by maintaining a low value of the coefficient of excess air α≤1.0, because this will lead to incomplete combustion of the fuel supplied to the muffle with the formation of products of incomplete combustion, including soot, which is unacceptable from the point of view of the activation process.

In addition to the above, the prototype has the following disadvantages:
- the steam-gas mixture obtained during the pyrolysis of coal is not used in the process as fuel, which reduces the technical and economic efficiency of the technology;
- neither chemical nor physical heat of activation gases is used in the process, which also reduces the technical and economic efficiency of the technology;
- for the drying of coal secondary heat of the process is not used, which is beneficial from the point of view of thermal efficiency of the process;
- there is no pyrolysis of the vapor-gas mixture, which increases the specific yield of semicoke and at the same time, freeing the vapor-gas mixture from the heaviest fractions of the resin, improves the properties of the vapor-gas mixture as fuel for use in muffles used in the technology;
- the conditions for mixing the coolant with the processed coal in the pyrolyzer are not provided.

 The aim of the invention is to eliminate these disadvantages of the prototype, improving the quality and quantity of activated carbons obtained, increasing the thermal efficiency of the process due to the efficient use of the gas-vapor mixture (ASG) obtained in the process as fuel and the recycling of secondary process heat in the technology.

 The claimed invention provides a simply implemented method for producing an activating gas that does not contain oxygen by filtering the ASG combustion products obtained in the activator muffle through a high-temperature fluidized bed of carbon-containing fine-grained material, in which there is a chemical interaction and binding of the oxygen contained in the gas to a carbon-containing material, in which part of the semi-coke or activated carbon obtained in the process is used to form carbon oxides.

 To achieve these goals, the method of thermal processing of fine-grained fuel involves drying the fuel with its subsequent separation from the drying agent, heating the dried fuel by mixing with the vapor-gas mixture, separating it from the vapor-gas mixture, supplying the deposited fuel to the solid heat carrier flow directed to the pyrolysis stage, and pyrolyzing the fuel into in a fluidized bed reactor with a solid coolant to obtain a semi-coke and a gas-vapor mixture, directed to mixing with fuel, feeding the semi-coke to the activator, heating it to the heeling layer with an activating agent with removal of the resulting solid phase of the finished product and receiving activation gases, returning one part of the heated solid phase to the pyrolysis stage as a solid heat carrier flow, supplying the second part of the solid phase to the lower gas distribution filtering fluidized bed additionally installed in the activator with feeding under it an activating agent, feeding a third part of the solid phase as a solid heat carrier into the gas volume of the reactor for mixing with the vapor-gas mixture, afterburning in the gas volume of the activator activating gas and forwarding them to a drying step.

 In addition, part of the vapor-gas mixture separated from the fuel is sent to an activating agent in an activator muffle.

 The third part of the solid phase is supplied as a solid coolant to the gas volume of the reactor by spraying.

 These goals are also achieved by the fact that the installation of thermal processing of solid fuel contains a dryer with a cyclone for separating fuel from a drying agent, a heat exchanger-adsorber equipped with a cyclone for separating fuel from a vapor-gas mixture and connected to the lower outlet of a cyclone serving to separate fuel from a drying agent, a fluidized bed pyrolysis reactor equipped with a steam-gas mixture outlet pipe connected to an adsorbing heat exchanger, a fluidized bed activator equipped with a main gas distribution top a casting grate, a muffle for producing an activating agent, a gas phase outlet pipe connected to the dryer inlet, and a finished product outlet pipe, a semi-coke transfer pipe, a solid coolant transfer pipe, connected to the lower outlet of the cyclone to separate the fuel from the vapor-gas mixture, and a transfer pipe solid phase connecting the fluidized bed of the activator with the gas volume of the pyrolysis reactor.

 In addition, the activator is equipped with a lower - additional gas distribution grid of the filtering fluidized bed installed between the main gas distribution grid and the muffle, a transfer pipe connecting the upper and lower boiling layers of the activator to supply part of the solid phase to the filtering fluidized bed, and means for supplying air blast to the gas volume of activator, located around the perimeter of the latter.

 The upper outlet of the cyclone for separating fuel from the gas mixture is connected to the activator muffle.

 The end of the solid-phase transfer piping located in the gas volume of the pyrolysis reactor is equipped with a baffle plate for distributing the solid phase supplied to the reactor over the reactor cross section.

 The drawing shows a diagram of the installation of thermal processing of solid fuel.

 The installation comprises a dryer 1, a cyclone 2 for precipitation of a solid phase, a heat exchanger-adsorber 3 connected to a dust exhaust pipe 5 of a cyclone 2 and equipped with a cyclone 4 for precipitation of coal from a gas-vapor mixture, a pyrolyzer reactor 6 with a fluidized bed, equipped with a gas-vapor mixture outlet pipe 7, connected to a heat exchanger-adsorber 3, a fluidized bed activator 8, a semi-coke transfer line 9, a solid transfer medium transfer pipe 10 for supplying a solid heat transfer medium to a pyrolysis reactor 6 with a dust removal cartridge connected thereto side assembly 11 of cyclone 4, a transfer pipe 12 connecting the fluidized bed of activator 8 with a gas volume 13 of reactor 6. The activator 8 is additionally equipped with a gas distribution grid 18 of a filter fluidized bed installed between the main gas distribution grid 14 and the muffle 15, a transfer pipe 19 connecting the upper and lower fluidized beds of activator 8 for supplying part of the solid phase to the filtering fluidized bed, and a manifold 20 provided with nozzles for supplying air blast into the gas volume of activator 8, located around the perimeter the last one. The upper outlet 21 of the cyclone 4 for deposition of fuel from the gas mixture is connected to the muffle 15 of the activator 8, and the dust outlet of the cyclone 4 is equipped with a device 22 for introducing fuel into the pipeline 10.

 The pyrolysis reactor 6 is equipped with cyclones 23 for purification of a gas-vapor mixture. The activator 8 is equipped with cyclones 24 for cleaning activation gases.

 The end of the transfer pipe 12, located in the gas volume 13 of the pyrolysis reactor 6, is equipped with a baffle plate 25.

 The technological process is as follows.

Fine-grained fuel, for example coal, with a particle size of 0-5 mm is fed into the dryer, in which the fuel is pre-dried from the initial moisture content of ~ 30% to a moisture content of 10-20% using exhaust gases of activator 8 having a temperature in the range of 750-900 ^o C. The dried fuel is separated from the drying agent in cyclone 2, the exhaust gases of which are sent to the furnace of the recovery boiler, and the coal deposited in cyclone 2 is fed to the heat exchanger-adsorber 3, in which the coal is dried to 3-5% humidity, while cooling the ASG and particles contained therein pulverized semi-coke and activated carbon, which adsorb heavy fractions of the resin from ASO.

 In cyclone 4, the coal is separated from the ASG and sent to the transfer line 10, in which it is mixed with the bulk of the solid coolant supplied from the activator 8 to the pyrolysis reactor 6, and together with the coolant enters the fluidized bed of the pyrolysis reactor 6. A smaller part of the solid phase is supplied from activator 8 to pyrolysis reactor 6 via line 12.

In reactor 6, coal is heated to a predetermined temperature of 500-600 ^o C (depending on the type of coal processed) and decomposes with the release of ASG, and the semi-coke obtained from coal is continuously removed from reactor 6 through pipeline 9 to activator 8 for processing it into activated carbon. The vapor distributed around the perimeter of the pyrolysis reactor 6 is fed to the lower part of the fluidized bed to stabilize the fluidized bed and improve the conditions for the semicoke removal and its partial activation.

Part of the solid heat carrier through the pipe 12 is fed into the gas volume 13 of the reactor and, using the baffle plate 25, is sprayed along the cross section of the gas volume 13 of the reactor, due to which it contacts the entire cross section of the reactor with the exhaust gas stream and ensures its overheating from 500-600 ^o С to 700 -800 ^o C and pyrolysis of the vapor contained in the ASG resin. As a result of this process, the content of the heaviest fractions of the resin decreases in PGS and at the same time the mass of the semi-coke obtained in the reactor increases due to the formation of resin coke during pyrolysis.

 Passing from top to bottom through the gas volume 13 of the reactor, the solid heat carrier is supplied to the fluidized bed of the reactor, in which it is mixed with the dried coal supplied to it.

 The ASO leaving the reactor passes through cyclones 23, in which it is partially dedusted, and the solid phase deposited in them is returned to the fluidized bed using risers.

 The circulation of the solid phase between the reactor 6 and the activator 8 is carried out through pipelines 10, 9 and 12 in a fluidized state due to the difference in hydrostatic pressure in the lower (pressure) and lifting (ascending) risers of the pipelines 10, 9 and 12, which is created by supplying water vapor to the lower part of the ascending pipelines, as shown in the drawing.

The exhaust gases of the reactor 6, consisting of steam-gas products of coal pyrolysis, from the cyclone 4 are fed into the furnace of the recovery boiler and partially into the muffle 15 of the activator 8, in which they are burned, and the resulting combustion products having a temperature of 800-900 ^o C, mixed with steam supplied to the muffle is used as an activating gas agent. Excess ASG is dumped into the furnace of the recovery boiler.

In order to free the residual oxygen obtained in the muffle 15 from the residual oxygen, the presence of which in the activating gases is unacceptable, since the presence of oxygen violates the normal course of the activation process, the obtained combustion products of the PGS in the muffle 15 before passing through the gas distribution grid of the activator 14 into the activation zone are passed through high-temperature (~ 800 ^o C), the fluidized bed filter, which is a fluidized bed of fine-grained carbonaceous material disposed on the gas distribution p lattice 18.

 The combustion products passing through the filtering fluidized bed and freed from oxygen, then pass through the grating 14 of the activator in the activation zone. In the fluidized bed, a chemical interaction of the flue gas oxygen with the carbon-containing material occurs.

 As the material of the filtering fluidized bed, the solid phase is used, which comes from the activation zone through the transfer pipe 19. As the carbon material is consumed (burned out), the fluidized bed is fed with the solid phase, for which, using the lower discharge valve 17, the material is periodically or continuously unloaded from a boiling filter layer. Unloaded waste material is a marketable product - activated carbon with slightly deteriorated characteristics due to a more macroporous structure (due to increased burning) and some increase in ash content.

 In the activator 8, the process of activation of the material coming into it from the pyrolysis reactor 6 in the form of a mixture of semicoke and solid heat transfer agent - activated carbon proceeds.

 An additional supply of heat to the fluidized bed of the activated material is carried out by burning the combustible components of the activation gases in the gas volume of the activator 8, into which air blast is supplied through the pipe 20 for this purpose. Commercial product - activated carbon is discharged from the fluidized bed of the activator periodically or continuously through the upper valve.

 Steam supply not only to the activation zone, but also to all transport communications of the semicoke and activated carbon and to the fluidized bed of the pyrolysis reactor facilitates the processes of semicoke activation.

An example implementation of the proposed method. The initial fine-grained coal (class 0-5 mm), for example brown coal of the Irsha-Borodinsky deposit of the Kansk-Achinsky basin, with the following characteristics (%): W ^r = 30.0; A ^d = 11.0; V ^daf = 47.0; S ^d = 0.3; Q ^r = 3650 kcal / kg is supplied to the aerosol dryer 1 in the amount of 4 t / h (performance of a typical pilot plant of this type). In the dryer, coal is dried from the initial humidity W = 30% to W≅18% due to the heat of the activator exhaust gases entering it with a temperature of ~ 750 ^o C.

 At the same time, ~ 600 kg / h of moisture evaporates from the coal, and dried coal after it is separated from the drying agent in cyclone 2 in an amount of 3230 kg / h enters the heat exchanger-adsorber 3. At the same time, ~ 5% of dried coal (~ 170 kg / h ) is carried away from cyclone 2 with the spent drying agent and enters the furnace of the recovery boiler.

 In the heat exchanger-adsorber 3, the coal is additionally dried to a moisture content of about 2.5%, while losing ~ 500 kg / h of moisture.

As a result, ~ 2600 kg / hr of dried coal enters the pyrolysis reactor 6, which, decomposing at a temperature of ~ 550 ^o C, releases ~ 900 kg / hr of a gas-vapor mixture (~ 30%) and forms ~ 1700 kg / hr of semi-coke (65%) . Part of the ASG from cyclone 4 is used as fuel in the muffle 15 of the activator 8 - from 200 to 400 kg / h - depending on the operating modes of the activator and the pyrolysis reactor. The excess part of ASG is burned in the furnace of the recovery boiler.

To heat 2600 kg / h of coal entering the pyrolysis reactor 6 from ~ 100 ^° C to 550 ^° C and to overheat the ASG from ~ 550 to 750 ^° C from the activator 8, a solid coolant in the amount of 3000 is continuously supplied to the pyrolyzer through pipelines 10 and 12 -4000 kg / h with a temperature of ~ 800 ^o C. The same amount of solid phase (semi-coke) is continuously discharged from reactor 6 to activator 8 through pipeline 9.

In the muffle 15 for the combustion of ASG and the formation of high-temperature activation gases (~ 800 ^o C) serves air blast in the amount of 1.5-3.0 thousand nm ³ / hour and water vapor in the amount of 1-2.0 thousand kg / hour .

 Of the 1700 kg / h of semi-coke obtained in the pyrolysis reactor, ~ 850 kg / h of activated carbon (with a burn of ~ 50%) is produced in the activator, which is removed from the activation zone, cooled and dispersed into fractions.

 The following are data confirming the receipt of technical results achieved by the invention in comparison with the closest analogue.

1. Improving the technical and economic efficiency of the technological process is achieved by feeding and burning a gas-vapor mixture in the muffle 15 of the activator 8 (paragraph 1 of the formula). The calculations were made for one ton of working fuel - coal of the Tugnuysky deposit: W _p = 30%; A = 15.7%; V ^g = 49.5%; Q = 7140 kcal / kg, based on the balance characteristics given in the closest analogue (RF patent 2074223, C 10 V 49/22, C 01 B 31/08 from 1997).

If 207 kg of a gas-vapor mixture (ASG) obtained from 1 t of raw coal (114 kg of tar with Q≅9000 kcal / kg and 93 kg of gas with Q≅5000 kcal / kg) is burned in an activator muffle, 1490000 kcal will be obtained. With partial resin pyrolysis, the thermal performance of ASG will decrease by no more than 15%, i.e. up to ~ 1.26 • 10 ⁶ kcal.

For overheating of 2700 kg of water vapor from 200 to 800 ^o C and heating to 800 ^o C, 2270 kg of semi-coke entering the activator (into the second reactor in analogous terminology) with a temperature of 550 ^o C requires ~ 950,000 kcal. Therefore, the heat received from the combustion of ASG is enough to carry out the indicated technological operations.

 The economic effect is equal to the cost of 100-150 kg of liquid fuel per 1 ton of processed coal.

 2. The use of heat from the activator 8 off-gas for pre-drying coal from ~ 30% to ~ 10% moisture and pre-heating it saves energy (heat) in the amount of ~ 150,000 kcal (per 1 ton of working fuel) that would have to be spent on external drying coal in a separate cycle.

 3. The pyrolysis of ASG provided in the invention in the volume of the reactor 13 (due to the supply and spraying of a high-temperature solid heat carrier - semi-coke) provides an increase in the yield of semi-coke by depositing tar coke on the surface of the particles of the semi-coke. With a total resin yield of 114 kg (per 1 ton of processed coal), heavy fractions in the resin of ~ 30% and the formation of resin coke in the amount of ~ 50% of the pyrolyzable resin, the yield of semicoke can be increased by ~ 5%.

 4. Based on the available experimental data, it was found that the complete elimination of oxygen from the activating vapor-gas mixture, which is achieved in this invention through the use of a special carbon filter, prevents excessive burning of the material and leads to the redistribution of the porous structure in favor of micro- and mesopores with a slight increase in the total volume pores and specific surface area of activated semicoke (see table).

Claims (5)

 1. The method of thermal processing of fine-grained fuel, including heating the fuel by mixing with the vapor-gas mixture, separating it from the vapor-gas mixture, pyrolyzing the fuel by heating it with a solid heat carrier in a fluidized bed reactor to obtain a semi-coke and vapor-gas mixture, directed to mixing with the fuel, feeding the semi-coke into activator, its heating in a fluidized bed with an activating agent with removal of the finished product and obtaining activation gases, the return of one part of the heated solid phase to the pyrolysis stage as a solid stream coolant, characterized in that the fuel is dried before mixing with the gas-vapor mixture, followed by separation of the drying agent, after separation from the gas-vapor mixture, it is introduced into the solid heat carrier stream returned to the pyrolysis stage, and a part of the gas-vapor mixture separated from the fuel is sent to obtain an activating agent in the muffle activator, the second part of the solid phase is sent to the gas distribution grid of the filtering fluidized bed additionally installed in the activator with the supply of activating a gent, the third part of the solid phase as a solid coolant is fed into the gas volume of the reactor for mixing with the vapor-gas mixture, and the activation gases obtained in the activator are burned in the gas volume of the activator and sent to the drying stage.  2. The method according to p. 1, characterized in that the supply of the third part of the solid phase as a solid coolant in the gas volume of the reactor is carried out by spraying.  3. Installation for the thermal processing of fine-grained fuel, containing a heat exchanger-adsorber with a cyclone for separating fuel from the gas-vapor mixture, a pyrolysis reactor with a fluidized bed, equipped with a pipe for outputting a gas-vapor mixture connected to a heat exchanger-adsorber, an activator with a fluidized bed, equipped with a gas distribution grid, a muffle to obtain an activating agent and nozzles for the output of the gas phase and the finished product, and transfer pipelines of semi-coke and solid coolant connecting the fluidized bed ak reactor and pyrolysis reactor, characterized in that the installation further comprises a dryer with a cyclone for separating fuel from the drying agent, the lower outlet of which is connected to the inlet to the heat exchanger-adsorber, a solid-state transfer pipe connecting the fluidized bed of the activator with the gas volume of the pyrolysis reactor, a cyclone for separating fuel from the vapor-gas mixture, the lower outlet of which is connected to a transfer line supplying solid coolant to the pyrolysis reactor, and the upper outlet is connected to the activator muffle RA, a pipe for withdrawing the gas phase from the activator is connected to the inlet to the dryer.  4. Installation according to claim 3, characterized in that the activator is additionally equipped with a gas distribution grid of the filtering fluidized bed installed between the main gas distribution grid and the muffle, a transfer pipe connecting the upper and lower fluidized layers of the activator to supply part of the solid phase to the lower filtering fluidized bed, and a collector for supplying air blast into the gas volume of the activator, located around the perimeter of the latter.  5. Installation according to claim 4, characterized in that the end of the transfer pipe supplying the solid coolant to the gas volume of the reactor is equipped with a baffle plate.

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