CN108949204B - Multistage thermal desorption device - Google Patents
Multistage thermal desorption device Download PDFInfo
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- CN108949204B CN108949204B CN201810754276.7A CN201810754276A CN108949204B CN 108949204 B CN108949204 B CN 108949204B CN 201810754276 A CN201810754276 A CN 201810754276A CN 108949204 B CN108949204 B CN 108949204B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
- C10B57/045—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing mineral oils, bitumen, tar or the like or mixtures thereof
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- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
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Abstract
A multi-stage thermal desorption device relates to the technical field of thermal desorption equipment and comprises a furnace body, a feeding pipe, a preheating zone, a dry distillation zone, a combustion zone, a cooling zone and a driving motor, wherein one end of the furnace body is communicated with the feeding pipe; the furnace body is provided with a steam outlet and a smoke outlet, the bottom end of the furnace body is provided with a slag discharge port, the discharge end of the furnace body is provided with an auxiliary burner, and the discharge end of the furnace body on the side opposite to the auxiliary burner is provided with a combustion air inlet pipe. The multistage thermal desorption device can separate the hydrocarbon gas flow with high quality, save energy and cost, and is suitable for large-scale popularization and use.
Description
The technical field is as follows:
the invention relates to the technical field of thermal desorption equipment, in particular to a multistage thermal desorption device.
Background art:
at present, a solid-liquid mixed waste rich in mineral oil, which is produced in the processes of petroleum exploration, exploitation, storage and transportation and refining, namely an oil-containing pollutant, wherein the oil-containing pollutant can cause serious pollution to the ecological environment or a water source no matter enters soil or oceans and lakes, and an effective and sustainable treatment is urgently needed, and the oil-containing pollutant causes great harm to the environment and human health, and an effective and sustainable treatment is urgently needed, wherein a thermal desorption technology is implemented worldwide, but the following problems exist: high investment cost of equipment, large energy consumption, low efficiency, low applicability of equipment, high operating cost and the like.
The invention content is as follows:
the invention aims to overcome the defects of the prior art and provide a multi-stage thermal desorption device which reduces energy consumption, is uniformly heated and easy to desorb, and achieves the purposes of economy and applicability.
In order to solve the problems existing in the background technology, the invention adopts the following technical scheme: the device comprises a furnace body, a feeding pipe, a preheating zone, a dry distillation zone, a combustion zone, a cooling zone and a driving motor, wherein one end of the furnace body is communicated with the feeding pipe, the preheating zone and the dry distillation zone are sequentially arranged in the furnace body from a feeding end to a discharging end, the cooling zone is formed between the preheating zone and the inner wall of the furnace body, the preheating zone consists of a plurality of heat conduction pipes which are symmetrically distributed, one end of each heat conduction pipe is connected with a rotating disc and penetrates through the rotating disc, the rotating disc is embedded on the inner wall of the furnace body, one side surface of the rotating disc is in sliding connection with the feeding pipe, the feeding pipe is communicated with the heat conduction pipes, the other end of each heat conduction pipe is fixedly connected with a feeding port of the dry distillation zone through a one-way sealing channel, the dry distillation zone is a cylindrical cavity, the dry distillation zone is fixedly connected with one end, a bidirectional sealing channel is arranged between the dry distillation zone and the combustion zone; a steam outlet is arranged on a cavity formed between the rotating disc and the feeding pipe; the furnace body is positioned at the top end of the preheating zone and is provided with a flue gas outlet, the furnace body is positioned at the bottom end of the preheating zone and is provided with a slag discharge port, the discharge end of the furnace body is provided with an auxiliary burner, and the discharge end of the furnace body on the side opposite to the auxiliary burner is provided with a combustion air inlet pipe.
The method comprises the following steps:
1) starting a driving motor, wherein the driving motor drives the preheating zone and the dry distillation zone to rotate in the furnace body, and the driving motor is driven by a variable frequency driver at the speed of 0.5-4.0 circles/minute;
2) the raw materials enter a heat conduction pipe of a preheating zone through a feeding pipe to be preheated, the rated operation pressure of the preheating zone is-7 to-3 mmWC, the preheating time is 9 to 11 minutes, and the preheating temperature is 200 to 300 ℃;
3) the method comprises the following steps that raw materials are preheated in a preheating zone and then enter a dry distillation zone through a one-way sealing channel for dry distillation, the rated operation pressure of the dry distillation zone is-50 to-30 mmWC, the raw materials are mixed with thermal cycle solids in the dry distillation zone for 2 to 4 minutes, wherein the self temperature of the thermal cycle solids is 700 to 800 ℃, and the mixed temperature is 400 to 600 ℃;
4) after the mixing temperature of the raw material and the thermal cycle solid reaches 400-600 ℃, the dry distillation work is completed, coke mixed in the raw material is deposited on the thermal cycle solid, two products are generated in the dry distillation process, namely hydrocarbon gas flow consisting of hydrocarbon gas and liquid fraction and granular coked carbon-containing solid, the hydrocarbon gas flow is conveyed into a specified recovery device through a clinker pipeline, and the carbon-containing solid enters a combustion area through a bidirectional sealed channel;
5) leaching the carbon-containing solid, and burning the carbon-containing solid in a burning zone, wherein the rated operating pressure of the burning zone is-20 to-10 mmWC, and the burning temperature in the burning zone is 700 to 800 ℃;
6) when the combustion heat in the combustion area is insufficient, combustion air enters the combustion area through the combustion air inlet pipe, and auxiliary combustion work is carried out on the combustion area through the auxiliary combustor, so that the combustion temperature of the combustion area reaches 700-800 ℃, and the combustion time is 4-6 minutes;
7) the solid and the flue gas after combustion in the combustion zone enter a cooling zone to be cooled, the solid and the flue gas with higher temperature after combustion in the combustion zone exchange heat with the raw materials in a heat conduction pipe in a preheating zone, namely the solid and the flue gas with higher temperature after combustion are heated by the raw materials in the heat conduction pipe through the pipe wall, the raw materials with lower temperature in the heat conduction pipe cool the solid and the flue gas with higher temperature, and the cooling time is 11-13 minutes;
8) when the solid and the flue gas are cooled to 300-500 ℃ in the cooling zone, the solid and the flue gas leave the cooling zone, water vapor generated by heat exchange is discharged through a steam outlet, the flue gas enters a flue gas treatment system through a flue gas outlet, and the solid enters a dust return system through a slag discharge port;
9) and finishing the multi-stage thermal desorption work.
The preheating zone and the dry distillation zone are in an oxygen-free environment.
The invention has the advantages of simple structure, environmental protection, gradual desorption through the preheating zone, the dry distillation zone and the combustion zone, and high-quality separation of hydrocarbon gas flow, so that pure hydrocarbon gas flow can be obtained; through the combustion area and the cooling area, the heating and cooling cyclic utilization work is realized, the purposes of saving energy and cost are further achieved, and the device is suitable for large-scale popularization and use.
Description of the drawings:
FIG. 1 is a schematic diagram of the present invention.
The specific implementation mode is as follows:
referring to fig. 1, the present invention specifically adopts the following embodiments: the device comprises a furnace body 1, a feeding pipe 2, a preheating zone 6, a dry distillation zone 7, a combustion zone 8, a cooling zone 4 and a driving motor, wherein one end of the furnace body 1 is communicated with the feeding pipe 2, the preheating zone 6 and the dry distillation zone 7 are sequentially arranged from a feeding end to a discharging end in the furnace body 1, the cooling zone 4 is formed between the preheating zone 6 and the inner wall of the furnace body 1, the preheating zone 6 consists of a plurality of heat conduction pipes which are symmetrically distributed, one end of each heat conduction pipe is connected with a rotating disc and penetrates through the rotating disc, the rotating disc is embedded on the inner wall of the furnace body 1, one side surface of the rotating disc is in sliding connection with the feeding pipe 2, the feeding pipe 2 is communicated with the heat conduction pipes, the other end of each heat conduction pipe is fixedly connected with a feeding port of the dry distillation zone 7 through a one-way sealing channel, the dry distillation zone 7, the material conveying pipeline 10 is connected with an output shaft of a driving motor, a combustion area 8 is formed between the dry distillation area 7 and the inner wall of the furnace body 1, and a bidirectional sealing channel is arranged between the dry distillation area 7 and the combustion area 8; the furnace body 1 is positioned on the top end of the preheating zone 6 and is sequentially provided with a steam outlet 3 and a flue gas outlet 5 from a feeding end to a discharging end, the furnace body 1 is positioned on the bottom end of the preheating zone 6 and is provided with a slag discharge port 12, the discharging end of the furnace body 1 is provided with an auxiliary burner 9, and the discharging end of the furnace body 1 on one side opposite to the auxiliary burner 9 is provided with a combustion air inlet pipe 11.
The method comprises the following steps:
1) starting a driving motor, wherein the driving motor drives the preheating zone 6 and the dry distillation zone 7 to rotate in the furnace body 1, and the driving motor is driven by a variable frequency driver at the speed of 0.5-4.0 circles/minute;
2) the raw materials enter a heat conduction pipe of a preheating zone 6 through a feeding pipe 2 to be preheated, the rated operation pressure of the preheating zone is-7 to-3 mmWC, the preheating time is 9 to 11 minutes, and the preheating temperature is 200 to 300 ℃;
3) the raw materials are preheated in a preheating zone 6 and then enter a dry distillation zone 7 through a one-way sealed channel for dry distillation, the rated operation pressure of the dry distillation zone 7 is-50 to-30 mmWC, the raw materials are mixed with thermal cycle solids in the dry distillation zone 7 for 2 to 4 minutes, wherein the self temperature of the thermal cycle solids is 700 to 800 ℃, and the mixed temperature is 400 to 600 ℃;
4) after the mixing temperature of the raw material and the thermal cycle solid reaches 400-600 ℃, the dry distillation work is completed, coke mixed in the raw material is deposited on the thermal cycle solid, two products are generated in the dry distillation process, namely hydrocarbon airflow and granular coked carbon-containing solid, the hydrocarbon airflow is respectively composed of hydrocarbon gas and liquid fraction, the hydrocarbon airflow is conveyed into a specified recovery device through a clinker pipeline 10, and the carbon-containing solid enters a combustion area 8 through a bidirectional sealed channel;
5) leaching the carbon-containing solid, and burning the carbon-containing solid in a burning zone 8, wherein the rated operating pressure of the burning zone 8 is-20 to-10 mmWC, and the burning temperature in the burning zone 8 is 700-800 ℃;
6) when the combustion heat in the combustion area 8 is insufficient, combustion air enters the combustion area 8 through the combustion air inlet pipe 11, and then auxiliary combustion work is carried out on the combustion area 8 through the auxiliary combustor 9, so that the combustion temperature of the combustion area 8 reaches 700-800 ℃, and the combustion time is 4-6 minutes;
7) the solid and the flue gas after combustion in the combustion zone 8 enter the cooling zone 4 for cooling, the solid and the flue gas with higher temperature after combustion in the combustion zone 8 exchange heat with the raw materials in the heat conduction pipe of the preheating zone 6, namely the solid and the flue gas with higher temperature after combustion are heated by the raw materials in the heat conduction pipe through the pipe wall, the solid and the flue gas with higher temperature are cooled by the raw materials with lower temperature in the heat conduction pipe, and the cooling time is 11-13 minutes;
8) when the solid and the flue gas are cooled to 300-500 ℃ in the cooling zone 4, the solid and the flue gas leave the cooling zone 4, the steam generated by heat exchange is discharged through the steam outlet 3, the flue gas enters the flue gas treatment system through the flue gas outlet 5, and the solid enters the dust return system through the slag discharge port 12;
9) and finishing the multi-stage thermal desorption work.
The preheating zone 6 and the dry distillation zone 7 are in an oxygen-free environment.
The multistage thermal desorption device, the preheating zone 6 and the dry distillation zone 7 run in an oxygen-free environment and are of a rotating structure, the driving motor is driven by a variable frequency driver, and the speed can be changed between 0.5 and 4.0 circles per minute.
The raw material first enters a preheating zone 6 of the furnace body 1, the rated operating pressure of the preheating zone 6 is-5 mmWC, and the preheating zone 6 consists of a plurality of same pipes which are symmetrically distributed. The raw material is heated in the preheating zone 6 to evaporate all free water; the steam produced in the preheating zone 6 and any air entrained with the feedstock is extracted from the preheating zone. The function of the preheating zone 6 is to dry and preheat the oily sludges to approximately 250 ℃ before they enter the retort zone, the heat being conducted through the walls of the heat pipes of the peripheral cooling zone. The preheated oil-containing sludge enters a dry distillation area 7.
The feedstock is in the retort zone 7 and is directly mixed with thermally recycled solids from the combustion zone 8, which thermally recycled solids provide heat to further heat the feedstock to retort temperatures. After dry distillation two products are produced, a hydrocarbon gas stream consisting of hydrocarbon gas and liquid fractions and a particulate carbonaceous solid. The hydrocarbon gas stream is withdrawn from the retort zone 7 and conveyed via a conveying line 10 to a designated recovery unit. The coked carbonaceous solids pass from the retort zone 7 to the combustion zone 8. The water content in the oily sludge is a main determinant factor of the processing capacity of the multistage pyrolysis desorption device. The reason is that the water in the feed affects the heat requirement in the preheat section to a large extent because of the large latent heat of evaporation in the water.
The dry distillation zone 7 is a cylindrical chamber, and oil-containing sludge (with the temperature of about 250 ℃) preheated from the preheating zone 6 flows into the dry distillation zone 7 through an internal one-way sealed channel along with the rotation of the interior of the multistage pyrolysis desorption device. The one-way sealed passage from the preheating zone 6 to the retort zone 7 only allows the passage of solids while preventing the flow of vapor between the preheating zone 6 and the retort zone 7. During the retorting in the retorting zone 7, a portion of the coke is deposited on the hot circulating solids. This coke serves as a source of process heat and is burned in the combustion zone. The excess heat demand is provided by auxiliary burners 9 on the combustion zone head side. The auxiliary burner 9 may ignite fuel oil to supplement the process heat. The rotation of the inner barrel also causes a mass of thermally cycled solids (at a temperature of about 740 c) to exit the combustion zone 8 from the bi-directional sealed tunnel and enter the retort zone 7. These thermally recycled solids are mixed with the feed from the preheating zone 6 with a degree of mixing after mixing of about 505 ℃. The dry distillation of the oily sludge produces hydrocarbon vapors, carbon-containing solids. Wherein the nominal operating pressure of the retort zone is-40 mmWC.
The combustion zone 8 provides part of the heat required by the multistage pyrolytic desorption unit by burning carbonaceous solids from the retort zone 7. When there is insufficient heat from the available carbonaceous solids, heat can be provided by auxiliary combustion, 9. The combustion air is preheated and then enters the combustion zone 8 through the combustion air inlet duct 11, and the combustion zone 8 is generally operated at a temperature of about 740 ℃ and a nominal operating pressure of-15 mmwc. The remaining solids of combustion enter the cooling zone 4 together with all combustion fumes.
The cooling zone 4 is an annular volume around the preheating zone 6. Hot flue gases and combusted carbonaceous solids enter from the combustion zone 8. Along with the rotation of the inner cylinder, the flue gas enters the flue gas treatment system through the flue gas outlet 5 and is discharged after being treated to be qualified. The waste slag enters a dust treatment system through a slag discharge port 12 for further treatment. They are cooled by the heat transfer of the feedstock in the preheating zone 6 through the walls of the heat conducting tubes of the preheating zone 6. In operation, the flue gases and solids leave the cooling zone 4 at a temperature of about 400 ℃. The cooling zone 4 and the preheating zone 6 of the multistage pyrolysis desorption apparatus function as counter-current heat exchangers. The hot waste solids and combustion flue gases transfer heat to the feedstock. The heat exchange is indirect, with heat being transferred from the cooling zone solids/flue gas to the preheating zone heat pipes and then to the feedstock. This completely isolates the hot waste solids from the feedstock.
The device can also be provided with a control system, and the control system can comprise a multistage pyrolysis desorption device control unit, an auxiliary burner control unit and a furnace body system. The auxiliary burner control unit and the furnace body system control the combustion amount in the combustion area 8 of the multi-stage pyrolysis desorption device. Changes in furnace equipment, combustion air rate, and/or disposer feed rate are used to control the temperature within combustion zone 8. The amount of combustion required by the burner depends on the nature of the feed oil-containing sludge, as this determines the amount of coke available on the solids after retorting. And the combustion-supporting fan provides combustion air for the combustion of the carbon-containing solids in the multistage pyrolysis desorption device. The furnace combustion and coke combustion air addition rates are controlled by a central control room and the operator can switch the multi-stage pyrolysis desorption unit control from full coke combustion mode to mixed combustion mode to maintain operating requirements and fuel balance.
In conclusion, the multistage thermal desorption device is simple in structure, green and environment-friendly, and the hydrocarbon gas flow is separated in high quality through stepwise desorption in the preheating zone 6, the dry distillation zone 7 and the combustion zone 8, so that pure hydrocarbon gas flow can be obtained; through the combustion zone 8 and the cooling zone 4, the heating and cooling cyclic utilization work is realized, the purposes of saving energy and saving cost are further achieved, and the device is suitable for large-scale popularization and use.
Claims (3)
1. The utility model provides a multistage thermal desorption device, includes furnace body (1), inlet pipe (2), preheating zone (6), dry distillation district (7), combustion area (8) and cooling zone (4) and driving motor, furnace body (1) one end and inlet pipe (2) intercommunication, furnace body (1) is inside to be equipped with preheating zone (6) and dry distillation district (7) to the discharge end by the feed end in proper order, forms cooling zone (4) between preheating zone (6) and furnace body (1) inner wall, its characterized in that: the preheating zone (6) is composed of a plurality of symmetrically distributed heat conduction pipes, one end of each heat conduction pipe is connected with the rotating disc and penetrates through the rotating disc, the rotating disc is embedded on the inner wall of the furnace body (1), the rotating disc and the feeding pipe (2) form a cavity, the other end of each heat conduction pipe is fixedly connected with a feeding hole of the dry distillation zone (7) through a one-way sealing channel, the dry distillation zone (7) is a cylindrical cavity, the dry distillation zone (7) is fixedly connected with one end of a material conveying pipeline (10), the other end of the material conveying pipeline (10) penetrates through the furnace body (1) to be connected with a recovery device, the material conveying pipeline (10) is connected with an output shaft of a driving motor, a combustion zone (8) is formed between the dry distillation zone (7) and the inner wall of the furnace body (1), and a two-; a steam outlet (3) is arranged in a cavity formed between the rotating disc and the feeding pipe (2); the furnace body (1) is positioned at the top end of the preheating zone (6) and is provided with a flue gas outlet (5), the furnace body (1) is positioned at the bottom end of the preheating zone (6) and is provided with a slag discharge port (12), an auxiliary burner (9) is arranged at the discharge end of the furnace body (1), and a combustion air inlet pipe (11) is arranged at the discharge end of the furnace body (1) on one side opposite to the auxiliary burner (9).
2. A method of using the multi-stage thermal desorption apparatus of claim 1, wherein: the method comprises the following steps:
1) starting a driving motor, wherein the driving motor drives the preheating zone (6) and the dry distillation zone (7) to rotate in the furnace body (1), and the driving motor is driven by a variable frequency driver at the speed of 0.5-4.0 circles/minute;
2) the raw materials enter a heat conduction pipe of a preheating zone (6) through a feeding pipe (2) for preheating, the rated operation pressure of the preheating zone is-7 to-3 mmWC, the preheating time is 9 to 11 minutes, and the preheating temperature is 200 to 300 ℃;
3) the raw materials are preheated in a preheating zone (6) and then enter a dry distillation zone (7) through a one-way sealed channel for dry distillation, the rated operation pressure of the dry distillation zone (7) is-50 to-30 mmWC, the raw materials are mixed with thermal cycle solids in the dry distillation zone (7) for 2 to 4 minutes, wherein the self temperature of the thermal cycle solids is 700 to 800 ℃, and the temperature after mixing is 400 to 600 ℃;
4) after the mixing temperature of the raw material and the thermal cycle solid reaches 400-600 ℃, the dry distillation work is completed, coke mixed in the raw material is deposited on the thermal cycle solid, two products are generated in the dry distillation process, namely hydrocarbon airflow and granular coked carbon-containing solid, the hydrocarbon airflow is respectively composed of hydrocarbon gas and liquid fraction, the hydrocarbon airflow is conveyed into a specified recovery device through a clinker pipeline (10), and the carbon-containing solid enters a combustion area (8) through a bidirectional sealed channel;
5) leaching carbon-containing solids, and burning the carbon-containing solids in a burning zone (8), wherein the rated operating pressure of the burning zone (8) is-20 to-10 mmWC, and the burning temperature in the burning zone (8) is 700 to 800 ℃;
6) when the combustion heat in the combustion area (8) is insufficient, combustion air enters the combustion area (8) through the combustion air inlet pipe (11), and then auxiliary combustion work is carried out on the combustion area (8) through the auxiliary combustor (9), so that the combustion temperature of the combustion area (8) reaches 700-800 ℃, and the combustion time is 4-6 minutes;
7) the solid and the flue gas after combustion in the combustion zone (8) enter a cooling zone (4) for cooling, the solid and the flue gas with higher temperature after combustion in the combustion zone (8) exchange heat with the raw materials in a heat conduction pipe of a preheating zone (6), namely the solid and the flue gas with higher temperature after combustion are heated by the raw materials in the heat conduction pipe through the pipe wall, the solid and the flue gas with higher temperature are cooled by the raw materials with lower temperature in the heat conduction pipe, and the cooling time is 11-13 minutes;
8) when the solid and the flue gas are cooled to 300-500 ℃ in the cooling area (4), the solid and the flue gas leave the cooling area (4), steam generated by heat exchange is discharged through the steam outlet (3), the flue gas enters the flue gas treatment system through the flue gas outlet (5), and the solid enters the dust return system through the slag discharge port (12);
9) and finishing the multi-stage thermal desorption work.
3. The multi-stage thermal desorption apparatus of claim 1, wherein: the preheating zone (6) and the dry distillation zone (7) are in an oxygen-free environment.
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