CN105018121A - Gas, tar and activated carton co-production system - Google Patents

Abstract

The invention discloses a gas, tar and activated carton co-production system. The system comprises a pyrolysis furnace, an activation furnace and a cooling furnace which are sequentially communicated. The pyrolysis furnace comprises a preheat furnace body and a pyrolysis furnace body, a coal inlet and a pyrolyzing gas outlet are formed in one end of the preheat furnace body, a heat-isolation jacket is disposed on the outer side of the activation furnace, and a heating chamber is formed between the activation furnace and the heat-isolation jacket; one end of the cooling furnace is connected with a discharge box, an activated carbon outlet and a cooling gas inlet are formed in the discharge box, a cooling jacket is arranged on the outer side of the cooling furnace, and a cooling chamber is formed between the cooling furnace and the cooling jacket; a cooling water inlet and a steam outlet are formed in the cooling jacket, and the steam outlet is communicated with the cooling gas inlet. Semicoke activated associated gas is used in the system to supply heat for pyrolysis, pyrolysis efficiency is improved, and meanwhile the content of nitrogen in pyrolysis gas is reduced. Mixed gas of carbon dioxide and water vapor can preheat the cooling furnace when passing through the cooling furnace and can prepare for being introduced in the activation furnace and serving as a gas activation agent, and activated carbon can be effectively cooled.

Description

Cogeneration system of gas, tar and activated carbon

technical field

The invention belongs to the technical field of pyrolysis gas, tar and activated carbon production, and in particular relates to a combined production system of pyrolysis gas, tar and activated carbon.

Background technique

Activated carbon is a kind of loose and porous carbonaceous material with adsorption effect, which is widely used in chemical industry, medicine, environmental protection and other industries. Semi-coke, that is, semi-coke, is a solid substance with high fixed carbon content produced by a medium-low temperature dry distillation process. During the production of semi-coke, tar and coke oven gas are by-products. Semi-coke can be widely used in calcium carbide, iron alloys , Activated carbon preparation and urban residents clean coal and other production and living fields. Tar has a wide range of uses and can be used to produce clean fuel oil. It is also an important raw material for organic chemicals such as synthetic plastics, dyes, fibers, rubber, pesticides, medicines, and high-temperature-resistant materials; coke oven gas can be used for power generation, metallurgy, hydrogen production, and ammonia synthesis. , methanol, stupid and other chemical products and heat sources for industrial calcination.

At present, coal carbonization technologies at home and abroad include: externally heated vertical furnace process, internally heated vertical furnace process, Toscoal process in the United States, LR process in Germany, 3TX (ETCH)-175 process in the former Soviet Union, fluidized bed rapid Pyrolysis process, China's multi-stage rotary furnace process, China's new dry distillation of solid heat carrier, Xi'an Sanrui Industrial Co., Ltd.'s external heating horizontal rotary carbonization furnace pyrolysis process, etc. The process of preparing semi-coke by thermal cracking in an internal heating vertical carbonization furnace is currently the most widely used, largest and largest process for cracking raw coal to prepare semi-coke. The process is mainly as follows: the raw coal is continuously and vertically fed into the coke oven from the coal hopper on the top of the furnace body, and then falls into the carbonization section after preheating. After mixing evenly in the fire channel, the blower blows it into the dry distillation section through the burner for combustion, and the coke in the lower part of the dry distillation section falls into the water-sealed tank to cool, and then is discharged. Raw coal gas rises along the material layer in the retort chamber, passes through the gas collection hood, rising pipe, and bridge pipe, and is washed by the Venturi tower and the swirl plate tower successively. The gas is returned to the furnace for heating under the action of the fan, and the remaining part is released. The tar enters the sedimentation tank for dehydration, and then concentrates in the tar pool for static heating and secondary dehydration. The dehydrated tar is the refined oil.

The disadvantages of the above method are:

1. Internal heating type dry distillation is adopted, and the furnace contains a large amount of air, so the generated gas has a low calorific value, contains low hydrogen, methane, and high nitrogen content, which cannot meet the best conditions for chemical utilization and can only be used as fuel .

2. The semi-coke is quenched by wet method, which consumes a part of the latent heat of semi-coke, and the product has a high water content, which affects the quality of semi-coke, limits the use of semi-coke, increases transportation costs, and consumes additional In addition, the waste steam generated during the coke quenching process contains a large amount of toxic and harmful substances, which deteriorates the on-site operating environment and pollutes the atmosphere; and the large amount of phenol-containing wastewater generated by coke quenching is expensive for post-treatment.

3. The tar recovery rate is low.

Contents of the invention

The purpose of the present invention is to overcome the deficiencies in the above-mentioned prior art and provide a cogeneration system of gas, tar and activated carbon. The cogeneration system uses semi-coke activated associated gas to provide heat for pyrolysis, which improves the pyrolysis efficiency and reduces the nitrogen content in the pyrolysis gas at the same time; Preheating prepares for passing through the activation furnace as a gas activator, and can also effectively cool the activated carbon.

In order to achieve the above object, the technical solution adopted by the present invention is: a co-production system of gas, tar and activated carbon, characterized in that it includes a pyrolysis furnace for preheating and pyrolysis of coal, and a pyrolysis furnace for pyrolysis An activation furnace for activating the generated semi-coke and a cooling furnace for cooling the activated carbon produced by activation, the pyrolysis furnace, activation furnace and cooling furnace are connected in sequence, and the pyrolysis furnace, activation furnace and cooling furnace are all It is a rotary furnace, the pyrolysis furnace includes a preheating furnace body and a pyrolysis furnace body connected with the preheating furnace body, and the end of the preheating furnace body away from the pyrolysis furnace body is provided with a coal inlet and a pyrolysis gas outlet , the outer side of the activation furnace is provided with a heat insulation jacket, a heating chamber for accommodating the activated heating gas is formed between the activation furnace and the heat insulation jacket, and the end of the cooling furnace far away from the activation furnace is connected with a discharge box, the discharge box is provided with an activated carbon outlet and a cooling gas inlet for introducing a mixture of water vapor and carbon dioxide into the discharge box, a cooling jacket is provided on the outside of the cooling furnace, and the cooling furnace and the A cooling chamber is formed between the cooling jackets, and a cooling water inlet and a steam outlet are provided on the cooling jacket, and both the cooling water inlet and the steam outlet lead to the cooling chamber, and the steam outlet and the The cooling gas inlets are connected.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that it includes a separation system for separating coal gas and tar from pyrolysis gas, and the separation system is connected to the outlet of the pyrolysis gas Pass.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that: the separation system includes a dust collector for removing dust in the pyrolysis gas, an indirect cooling system for condensing the pyrolysis gas device and an electric tar collector for trapping the oil-water mixture formed after the pyrolysis gas is condensed, and an absorption tower and a desorption tower for capturing carbon dioxide in the pyrolysis gas by using the MEA solution, the pyrolysis gas The outlet is connected to the bottom of the dust collector, the top of the dust collector is connected to the bottom of the indirect cooler, the top of the indirect cooler is connected to the bottom of the electric tar catcher, and the top of the electric tar catcher is connected to the absorption The bottom of the tower is connected, the bottom of the absorption tower is connected with the top of the desorption tower, the bottom of the desorption tower is connected with the top of the absorption tower, the top of the absorption tower is provided with a gas outlet, and the desorption tower The top of the electric tar catcher is provided with a carbon dioxide outlet, and the bottom of the electric tar catcher is connected with a tar storage tank.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that: the separation system also includes a tar ammonia water clarifier for collecting the oil-water mixture in the indirect cooler and separating tar, and the tar ammonia water The clarifier is provided with a tar output port, a tar residue output port and an ammonia water discharge port.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that: the tar ammonia water clarification tank is a sealed ammonia water tank.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that: the indirect cooler is a tube-and-tube heat exchanger.

The above-mentioned cogeneration system of pyrolysis gas, tar and activated carbon is characterized in that: the dust collector is a high-temperature cyclone dust collector.

Compared with the prior art, the present invention has the following advantages:

1. The structure of the present invention is simple, and the design is novel and reasonable.

2. The present invention indirectly heats the semi-coke in the activation furnace by setting a heating chamber, avoiding the use of burning semi-coke to provide an activation heat source, thereby increasing the production capacity of activated carbon, and improving the quality of activated carbon, replacing the air in the prior art The heating mode of the combustion chamber reduces the nitrogen content in the gas.

3. When the present invention cools the activated carbon, by combining the indirect cooling method and the direct cooling direction, the activated carbon can be fully and completely cooled, and the moisture content of the activated carbon can be ensured to be low, thereby improving the quality of the activated carbon.

4. The present invention can effectively separate tar and coal gas from the pyrolysis gas through the separation system, and can increase the calorific value of the gas through the capture of carbon dioxide, and at the same time reduce the emission of carbon dioxide, avoiding the impact of the presence of carbon dioxide on The impact of gas calorific value.

5. The separation system of the present invention can further process the oil-water mixture formed by the condensation of the pyrolysis gas in the indirect cooler by setting the tar ammonia water clarification tank, effectively separate the tar from the oil-water mixture, and improve the production of tar. rates and recovery rates.

6. The dust collector of the present invention adopts a high-temperature cyclone dust collector. By adopting a high-temperature cyclone dust collector, it can ensure that the temperature inside the dust collector is at a high temperature, so as to effectively reduce the condensation of heavy oil in the dust collector.

7. The pulverized coal whose raw material particle size is less than or equal to 6mm in the present invention can make full use of small particle size coal.

The technical solutions of the present invention will be described in further detail below with reference to the accompanying drawings and embodiments.

Description of drawings

Fig. 1 is a structural schematic diagram of the present invention.

Fig. 2 is a sectional view of A-A in Fig. 1 .

Fig. 3 is a B-B sectional view in Fig. 1 .

Explanation of reference signs:

1—pyrolysis furnace; 1-1—preheating furnace body; 1-2—pyrolysis furnace body;

1-3—coal inlet; 1-4—pyrolysis gas outlet; 1-5—power device;

1-6—big gear; 1-7—the first roller; 1-8—the first roller seat;

2—activation furnace; 2-1—the second supporting wheel; 2-2—the second supporting wheel seat;

2-3—the first support; 3—heat insulation jacket; 3-1—activated heating gas inlet;

3-2—activated heating gas outlet; 4—heating chamber; 5—cooling jacket;

5-1—cooling water inlet; 5-2—steam outlet; 6—cooling chamber;

7—cooling furnace; 7-1—the third supporting wheel; 7-2—the third supporting wheel seat;

7-3—the second support; 8—discharge box; 8-1—activated carbon outlet;

8-2—cooling gas inlet; 9—dust collector; 10—indirect cooler;

11—electric tar catcher; 12—absorption tower; 12-1—gas outlet;

13—desorption tower; 13-1—carbon dioxide outlet; 14—carbon dioxide storage tank;

15—tar storage tank; 16—tar intermediate tank; 17—tar residue tank;

18—tar ammonia water clarification tank; 19—ammonia water recovery tank.

Detailed ways

A cogeneration system of gas, tar and activated carbon as shown in Figure 1, Figure 2 and Figure 3, including a pyrolysis furnace 1 for preheating and pyrolyzing coal, semi-coke for pyrolysis The activation furnace 2 for activation and the cooling furnace 7 for cooling the activated carbon produced by activation, the pyrolysis furnace 1, the activation furnace 2 and the cooling furnace 7 are connected successively, and the pyrolysis furnace 1, the activation furnace 2 and the The cooling furnace 7 is a rotary furnace, and the pyrolysis furnace 1 includes a preheating furnace body 1-1 and a pyrolysis furnace body 1-2 communicated with the preheating furnace body 1-1, and the preheating furnace body 1-1 One end away from the pyrolysis furnace body 1-2 is provided with a coal inlet 1-3 and a pyrolysis gas outlet 1-4, and the outer side of the activation furnace 2 is provided with a heat insulation jacket 3, and the activation furnace 2 is insulated from the heat insulation A heating chamber 4 for accommodating activated heating gas is formed between the jackets 3, wherein an activated heating gas inlet 3-1 and an activated heating gas outlet 3-2 are opened on the heat insulating jacket 3, and the activated heating gas The gas inlet 3-1 and the activated heating gas outlet 3-2 all lead to the heating chamber 4, and the end of the cooling furnace 7 away from the activation furnace 2 is connected with a discharge box 8, and the discharge box 8 is provided with Activated carbon outlet 8-1 and the cooling gas inlet 8-2 that is used to pass into water vapor and carbon dioxide mixed gas in the discharge box 8, the outside of described cooling furnace 7 is provided with cooling jacket 5, described cooling furnace 7 and all A cooling chamber 6 is formed between the cooling jackets 5, and a cooling water inlet 5-1 and a steam outlet 5-2 are provided on the cooling jacket 5, and the cooling water inlet 5-1 and the steam outlet 5-2 are both Leading to the cooling chamber 6, the steam outlet 5-2 communicates with the cooling gas inlet 8-2.

In this embodiment, when the cogeneration system is in use, the pyrolysis furnace 1, the activation furnace 2 and the cooling furnace 7 rotate synchronously, and pulverized coal is fed into the preheating furnace body 1 of the pyrolysis furnace 1 from the coal inlet 1-3 In -1, the preheated pulverized coal enters the pyrolysis furnace body 1-2 of the pyrolysis furnace 1, and the pulverized coal is pyrolyzed in the pyrolysis furnace body 1-2 to produce pyrolysis gas and semi-coke, wherein the pyrolysis The gas is output from the pyrolysis gas outlet 1-4 to further separate the gas and tar, wherein the semi-coke enters the activation furnace 2 to be activated to produce activated carbon, and the activated carbon enters the cooling furnace 7 to cool and then enters the discharge box 8.

In this embodiment, the cogeneration system indirectly heats the semi-coke in the activation furnace 2 by setting the heating chamber 4, avoiding the use of burning semi-coke to provide the activation heat source, thereby increasing the production capacity of activated carbon and improving the quality of activated carbon. It replaces the air combustion chamber heating mode in the prior art, and reduces the nitrogen content in the gas. In addition, the associated gas generated in the activation furnace 2 enters the pyrolysis furnace body 1-2 to provide heat for the pyrolysis of pulverized coal, and then enters the preheating furnace body 1-1 to provide heat for the preheating of pulverized coal. In this embodiment, since the gas activator passed into the activation furnace 2 is a mixed gas of water vapor and carbon dioxide, in the process of semi-coke activation, an associated gas, namely a mixed gas of CO and H ₂ is produced, and the associated gas The H ₂ contained in the gas can further realize hydropyrolysis, which greatly improves the yield of tar and the quality of gas. The mixed gas of water vapor and carbon dioxide is passed into the discharge box 8 and then directly cooled by contacting the activated carbon through the cooling furnace 7. The mixed gas of water vapor and carbon dioxide is also preheated while cooling the activated carbon and then enters the activation furnace 2 as a gas Activator used. Moreover, when the cogeneration system cools the activated carbon, the cooling effect on the activated carbon is greatly increased by combining the indirect cooling method and the direct cooling direction. The direct cooling of activated carbon in 7, the indirect cooling method is to pass cooling water into the cooling chamber 6 through the cooling water inlet 5-1, and the cooling water indirectly cools the activated carbon in the cooling furnace 7 in a non-contact manner. While cooling the activated carbon, the cooling water is heated into steam form and sent from the steam outlet 5-2 into the cooling gas inlet 8-2 to be mixed with carbon dioxide to form cooling gas for direct cooling.

In this embodiment, the pyrolysis furnace 1, the activation furnace 2 and the cooling furnace 7 are sequentially connected and synchronized during rotation, so the pyrolysis furnace 1, the activation furnace 2 and the cooling furnace 7 only need one power unit 1- 5, the power unit 1-5 drives the large gear 1-6 on the pyrolysis furnace 1, and the large gear 1-6 drives the preheating furnace body 1-1 and the pyrolysis furnace body 1 of the pyrolysis furnace 1 -2 rotation, both ends of the pyrolysis furnace 1 are provided with a first supporting wheel 1-7 and a first supporting wheel seat 1-8 matched with the first supporting wheel 1-7. The part of the activation furnace 2 close to the pyrolysis furnace 1 is provided with a second supporting wheel 2-1 and a second supporting wheel seat 2-2 matched with the second supporting wheel 2-1. The part of the cooling furnace 7 close to the discharge box 8 is provided with a third supporting roller 7-1 and a third supporting roller seat 7-2 matched with the third supporting roller 7-1. The bottom of the activation furnace 2 is provided with a first support 2-3, and the bottom of the cooling furnace 7 is provided with a second support 7-3. Wherein, the power device 1-5 includes a motor and a reducer connected to the motor, and a pinion gear meshing with the bull gear 1-6 is installed on the output shaft of the reducer.

In this embodiment, the cogeneration system further includes a separation system for separating coal gas and tar from the pyrolysis gas, and the separation system is connected to the pyrolysis gas outlet 1-4.

As shown in Figure 1, the separation system includes a dust collector 9 for removing dust in the pyrolysis gas, an indirect cooler 10 for condensing the pyrolysis gas, and an indirect cooler 10 for condensing the pyrolysis gas. An electric tar catcher 11 for collecting tar from an oil-water mixture, and an absorption tower 12 and a desorption tower 13 for trapping carbon dioxide in the pyrolysis gas using MEA solution, the pyrolysis gas outlets 1-4 are connected to the bottom of the dust collector 9 The top of the dust collector 9 is connected with the bottom of the indirect cooler 10, the top of the indirect cooler 10 is connected with the bottom of the electric tar catcher 11, and the top of the electric tar catcher 11 is connected with the absorption The bottom of tower 12 is connected, and the bottom of described absorption tower 12 is connected with the top of described desorption tower 13, and the bottom of described desorption tower 13 is connected with the top of absorption tower 12, and the top of described absorption tower 12 is provided with gas Outlet 12-1, the top of the desorption tower 13 is provided with a carbon dioxide outlet 13-1, and the bottom of the electric tar collector 11 is connected with a tar storage tank 15.

In this embodiment, when the separation system is in use, the dust in the pyrolysis gas is first effectively intercepted by the dust collector 9, and then the pyrolysis gas is condensed by the indirect cooler 10, and the pyrolysis gas is condensed to form an oil-water mixture and Low-temperature gas, wherein the low-temperature gas enters into the electric tar catcher 11 for tar capture to remove the tar in the low-temperature gas, the tar captured in the electric tar catcher 11 is transported to the tar storage tank 15, and the remaining gas enters At the bottom of the absorption tower 12, the gas flows from bottom to top, and the lean liquid flows continuously from the top of the absorption tower 12 from top to bottom, and contacts with the gas flowing upwards. The carbon dioxide in the gas reacts with the MEA solution, and the carbon dioxide is absorbed by the MEA. Solution absorption, the purified gas is output from the gas outlet 12-1 at the top of the absorption tower 12, while the carbon dioxide is being absorbed, the liquid releases heat of reaction, and the rich liquid is sent to the top of the desorption tower 13, and the desorption tower 13 is reboiled The device provides heat to generate a large amount of steam. The steam flows upward in the desorption tower 13 and contacts the flowing rich liquid. After the rich liquid is heated and stripped, carbon dioxide is gradually desorbed and released from the rich liquid, and the rich liquid becomes The lean liquid is transported from the bottom of the desorption tower 13 to the top of the absorption tower 12 for reuse, and the desorbed carbon dioxide is transported to the carbon dioxide storage tank 14 from the carbon dioxide outlet 13-1 at the top of the desorption tower 13, and then becomes an activation furnace. Activation of the inner coke provides the activator.

In this embodiment, the separation system can increase the calorific value of the gas by capturing carbon dioxide, and at the same time reduce the emission of carbon dioxide, avoiding the influence of the presence of carbon dioxide on the calorific value of the gas.

As shown in Figure 1, the separation system also includes a tar ammonia water clarifier 18 for collecting the oil-water mixture at the bottom of the indirect cooler 10 and separating tar, and the tar ammonia water clarifier 18 is provided with a tar output port and a tar residue output. mouth and ammonia outlet. The oil-water mixture formed by the condensation of the pyrolysis gas in the indirect cooler 10 can be further processed by setting the tar ammonia water clarification tank 18, and the tar is effectively separated from the oil-water mixture, thereby increasing the yield of the tar. Wherein, the tar output port is connected with a tar intermediate tank 16, the tar intermediate tank 16 is connected with the tar storage tank 15, the tar residue output port is connected with a tar residue tank 17, and the ammonia water outlet is connected with an ammonia recovery Groove 19.

In this embodiment, the tar ammonia water clarification tank 18 is a sealed ammonia water tank. The indirect cooler 10 is a shell and tube heat exchanger.

In this embodiment, the dust collector 9 is a high-temperature cyclone dust collector. By adopting a high-temperature cyclone dust collector, it can ensure that the temperature inside the dust collector 9 is at a high temperature, so as to effectively reduce the condensation of heavy oil in the dust collector 9 .

The above are only preferred embodiments of the present invention, and are not intended to limit the present invention. Any simple modifications, changes and equivalent structural transformations made to the above embodiments according to the technical essence of the present invention still belong to the present invention. within the protection scope of the technical solution.

Claims (7)

1. A co-production system of coal gas, tar and activated carbon, characterized in that: comprising a pyrolysis furnace (1) for preheating and pyrolysis of coal, an activation furnace for activating the semi-coke produced by pyrolysis Furnace (2) and the cooling furnace (7) that is used for cooling the active carbon that activation produces, described pyrolysis furnace (1), activation furnace (2) and cooling furnace (7) communicate successively, and described pyrolysis furnace (1), the activation furnace (2) and the cooling furnace (7) are all rotary furnaces, and the pyrolysis furnace (1) includes a preheating furnace body (1-1) and communicates with the preheating furnace body (1-1) A pyrolysis furnace body (1-2), the end of the preheating furnace body (1-1) away from the pyrolysis furnace body (1-2) is provided with a coal inlet (1-3) and a pyrolysis gas outlet ( 1-4), the outer side of the activation furnace (2) is provided with a thermal insulation jacket (3), between the activation furnace (2) and the thermal insulation jacket (3) constitutes a heating chamber for accommodating the activated heating gas chamber (4), the end of the cooling furnace (7) away from the activation furnace (2) is connected with a discharge box (8), and the discharge box (8) is provided with an activated carbon outlet (8-1) and a Pass into the cooling gas inlet (8-2) of steam and carbon dioxide mixed gas in the discharge box (8), the outside of described cooling furnace (7) is provided with cooling jacket (5), described cooling furnace (7) ) and the cooling jacket (5) form a cooling chamber (6), the cooling jacket (5) is provided with a cooling water inlet (5-1) and a steam outlet (5-2), the Both the cooling water inlet (5-1) and the steam outlet (5-2) lead to the cooling chamber (6), and the steam outlet (5-2) communicates with the cooling gas inlet (8-2) . 2. The cogeneration system of a kind of pyrolysis gas, tar and active carbon according to claim 1, is characterized in that: comprise the separation system that is used to separate coal gas and tar from pyrolysis gas, described separation system and The pyrolysis gas outlets (1-4) are connected. 3. a kind of cogeneration system of pyrolysis gas, tar and gac according to claim 2, is characterized in that: described separation system comprises the dust catcher (9) that is used to remove the dust in pyrolysis gas, for The indirect cooler (10) for condensing the pyrolysis gas and the electric tar collector (11) for trapping the oil-water mixture formed after the pyrolysis gas is condensed, and using the MEA solution to treat the tar in the pyrolysis gas An absorption tower (12) and a desorption tower (13) for capturing carbon dioxide, the pyrolysis gas outlet (1-4) communicates with the bottom of the dust remover (9), and the top of the dust remover (9) is connected with the indirect cooling The bottom of device (10) is communicated, and the top of described indirect cooler (10) is communicated with the bottom of electric tar catcher (11), and the top of described electric tar catcher (11) is connected with the absorption tower (12) The bottom is connected, the bottom of the absorption tower (12) is connected with the top of the desorption tower (13), the bottom of the desorption tower (13) is connected with the top of the absorption tower (12), and the absorption tower ( The top of 12) is provided with gas outlet (12-1), the top of described desorption tower (13) is provided with carbon dioxide outlet (13-1), and the bottom of described electric tar catcher (11) is connected with tar storage tank ( 15). 4. The cogeneration system of a kind of pyrolysis gas, tar and activated carbon according to claim 3, characterized in that: the separation system also includes an oil-water mixture for collecting the indirect cooler (10) and separating the tar A tar ammonia water clarification tank (18), the tar ammonia water clarification tank (18) offers a tar output port, a tar residue output port and an ammonia water discharge port. 5. A cogeneration system of pyrolysis gas, tar and activated carbon according to claim 4, characterized in that: the tar ammonia water clarification tank (18) is a sealed ammonia water tank. 6. A cogeneration system of pyrolysis gas, tar and activated carbon according to claim 3, characterized in that: the indirect cooler (10) is a tube-and-tube heat exchanger. 7. A cogeneration system of pyrolysis gas, tar and activated carbon according to claim 3, characterized in that: the dust collector (9) is a high-temperature cyclone dust collector.