WO2014094308A1

WO2014094308A1 - Pyrolysis gasification method and device for preparing tar-free hydrogen-rich gas

Info

Publication number: WO2014094308A1
Application number: PCT/CN2012/087190
Authority: WO
Inventors: 许光文; 韩江则; 曾玺; 高士秋; 董鹏伟
Original assignee: 中国科学院过程工程研究所
Priority date: 2012-12-21
Filing date: 2012-12-21
Publication date: 2014-06-26

Abstract

The present invention relates to a pyrolysis gasification method and device for preparing a tar-free hydrogen-rich gas, the pyrolysis gasification method comprising the following steps: 1) transferring via a feeding device a carbonic solid raw material into an upstream pyrolysis reactor for aerobic pyrolysis to generate a pyrolyzed gas-phase product and a solid product; 2) transferring the pyrolyzed gas-phase product and solid product generated in step 1) into a downstream tar pyrolysis reactor; removing the tar through high temperature pyrolysis, partial oxidization and carbocoal pyrolysis catalytic lytic reaction; and simultaneously, pyrolyzing and gasifying a part of the carbocoal to obtain a pyrolyzed gas and pyrolyzed carbocoal. The present invention avoids the problems of low H₂ and CH₄ content in the pyrolyzed gas and large treatment workload in a subsequent gas composition reforming reaction due to the fact that in the prior art a volatile component is also burned when the fuel burns to supply heat energy.

Description

Pyrolysis gasification method for preparing tar-free hydrogen-rich gas and pyrolysis gasification device

Technical field

The present invention relates to the field of solid fuel energy chemical technology, and in particular, to a pyrolysis gasification method and a pyrolysis gasification apparatus for preparing a tar-free hydrogen-rich gas. Background technique

Gasification of carbonaceous solid fuels (coal, biomass and other carbonaceous solid wastes, etc.) is an important means of utilization. At present, the gasification process of industrial operation generally adopts an autothermal process, that is, the heat required in the gasification reaction process is provided by burning a part of the gasification raw material. Since the reaction temperature during the entire gasification process is high, it is necessary to burn more than 40% of the carbonaceous raw material to maintain the temperature required for the reaction (above lolcrc). In the process, not only a part of the gasification raw material is burned, but also a useful gas component such as H ₂ , CH ₄ or the like is also burned, resulting in 11⁄2 / of the obtained gas. The ratio of 0 is greatly reduced. As a highly efficient and clean gas resource, there is a large demand in the following processes such as the synthesis of formazan and ammonia. Taking synthetic formam as an example: In the actual production, H ₂ /CO=3.0 is required in the raw material gas, and the Lurg furnace process with the highest H ₂ /CO ratio in the gas composition of the current gasification process is only about 1.6. Therefore, in order to meet the needs of subsequent industrial production, it is necessary to carry out a reforming reaction on the obtained atmosphere to adjust the composition of the gas. The entire process is cumbersome and complicated, and is accompanied by a lot of energy consumption. Although the content of 13⁄4 in the gas produced by the coal-based blue carbon process is greatly increased, at the same time, a large amount of tar is associated with the obtained dry distillation gas, which results in a complicated gas purification process and poor operation stability of the equipment. In order to solve the above problems, some research has been carried out. For example, the patent: CN101045525 proposes that in a spouted bed or a fluidized bed reactor under high pressure conditions, water vapor is used as a gasification gas, and carbon dioxide is completely absorbed by adding a carbon dioxide absorbent. The purpose of increasing hydrogen yield. However, the process is carried out under high pressure conditions, in which the carbon dioxide absorber KOH or Ca(OH) ₂ agglomerates seriously, affecting the normal operation of the process. At the same time, the tar production situation and the treatment method in the whole process are not mentioned.

From the above analysis, we can see that the gasification process urgently needs to be solved: First, try to increase the content of high-quality gases such as H ₂ and CH ₄ in the gasification gas to increase the H ₂ /CO ratio and reduce the subsequent reforming reaction. The second is to remove the tar from the obtained gasification gas to the utmost extent. Summary of the invention

SUMMARY OF THE INVENTION An object of the present invention is to provide a pyrolysis gasification method for preparing a tar-free hydrogen-rich gas in order to solve the above problems. Another object of the present invention is to provide a pyrolysis gasification apparatus based on the above-described pyrolysis gasification method for preparing a tar-free hydrogen-rich gas.

The pyrolysis gasification method for preparing a tar-free hydrogen-rich gas of the present invention comprises the following steps:

1) feeding the carbonaceous solid raw material into the upstream pyrolysis reactor through a feeding device for aerobic pyrolysis to produce a pyrolysis gas phase product and a solid product;

2) The pyrolysis gas phase product and the solid product produced in the step 1) are passed into a downstream tar cracking reactor, and the tar is removed by high temperature thermal cracking, partial oxidation and pyrolysis semi-coke catalytic cracking reaction, and partial gas is generated by pyrolysis of the semi-coke. The reaction is carried out to obtain pyrolysis gas and pyrolysis semi-coke.

According to the pyrolysis gasification method of the present invention, the carbonaceous solid raw material is coal, biomass or other carbonaceous solid waste or the like.

According to the pyrolysis gasification method of the present invention, the reaction temperature in the upstream pyrolysis reactor is 700-1000 ° C, and the heat can be obtained by using an external heat type, that is, by burning fuel or passing outside the upstream pyrolysis reactor. The hot flue gas is used to provide the heat required for the reaction, and can be obtained by self-heating, that is, by using a portion of oxygen/air or the like to be reacted with the reaction raw material to release the heat released by the reaction; the downstream tar cracking reactor The internal reaction temperature is 900-130 CTC, which is maintained by the heat from the upstream overflow material itself and the heat released by the oxygen-containing atmosphere and the semi-coke reaction. The above specific reaction temperatures can be adjusted according to different reaction materials.

According to the pyrolysis gasification method of the present invention, the pyrolysis gas obtained in the step 2) is subjected to gas-solid separation; after the pyrolysis semi-coke obtained in the step 2) is quenched, waste heat recovery is performed. Specifically, it can be connected to the quenching device 8 during the semi-coke discharge process at the same time, and high-temperature and high-pressure steam is generated by heat exchange, and the heat carried by the semi-coke is recovered while the temperature of the semi-coke is lowered.

According to the pyrolysis gasification process of the present invention, an appropriate amount of calcium-based minerals or other minerals or catalysts having tar cracking ability can be added to the pyrolysis feedstock.

The pyrolysis gasification method for producing a tar-free hydrogen-rich gas of the present invention can be carried out under normal pressure and under pressure.

The pyrolysis gasification apparatus of the present invention based on the pyrolysis gasification method for preparing a tar-free hydrogen-rich gas, comprising a feeding device 1, an overflow pipe 3, and an upstream pyrolysis reactor 2 and a downstream tar cracking reactor 4 The two are connected by an overflow pipe 3, and the feeding device 1 is in communication with the upstream pyrolysis reactor 2.

According to the pyrolysis gasification apparatus of the present invention, the upstream pyrolysis reactor is preferably a rotary kiln, a fluidized bed or a dilute phase transport bed; the downstream tar cracking reactor is preferably a rotary kiln, a dilute phase transport bed, a settling furnace Or a fixed bed. The pyrolysis gasification apparatus according to the present invention may further include a cyclone separator 5, a material leg 6, a discharge tube 7 and a quenching device 8, respectively, and the downstream tar cracking reactor 4 and the quenching device 8 phases are connected, the upper material inlet of the cyclone separator 5 is connected to the quenching device 8 through a pipe, and the solid product outlet at the bottom of the cyclone separator 5 is connected to the solid product collecting device through the material leg 6.

Based on the pyrolysis gasification apparatus described above, the following methods may be preferred:

The upstream pyrolysis reactor may be a first rotary kiln reactor 13, and the downstream tar cracking reactor is a second rotary kiln reactor 14.

The upstream pyrolysis reactor may be a fluidized bed 10 and the downstream tar cracking reactor is a second rotary kiln reactor 14. Further, the fluidized bed 10 can also be connected to a plurality of second rotary kiln reactors 14 to form a device group.

The upstream pyrolysis reactor may be a dilute phase transport bed 11, and the downstream tar cracking reactor is a second rotary kiln reactor 14.

In addition to the above-mentioned cyclone separator 5, the material leg 6, the defocusing tube 7 and the quenching device 8, the cyclone separator 5, the material leg 6, and the quenching device 8 may be further included, the cyclone separator 5 The upper material inlet is in communication with the downstream tar cracking reactor 4 via a conduit, and the solid product outlet at the bottom of the cyclone separator 5 is in communication with the quenching device 8 via the feed leg 6.

The upstream pyrolysis reactor is a fluidized bed 10, and the downstream tar cracking reactor may be a dilute phase transport bed 11.

The upstream pyrolysis reactor is a fluidized bed 10, and the downstream tar cracking reactor may be a settling furnace

12.

Further, preferably, the gas outlet at the lower side of the side wall of the settling furnace 12 is in communication with the inlet of the cyclone separator 5, and the bottom of the settling furnace 12 is directly in communication with the quenching device 8.

In the above pyrolysis gasification method for preparing a tar-free hydrogen-rich gas and the pyrolysis gasification apparatus, the supply device 1 is preferably a screw feed device.

The main idea of the invention is to first extract the volatile matter in the carbonaceous solid fuel by pyrolysis, and then further remove the tar in the pyrolysis gas, partially vaporize the semi-coke, and adjust the conversion of the composition of the pyrolysis atmosphere. The reactions are coupled together to increase the content of high quality components (H ₂ , CH _{4 ,} etc.) in the pyrolysis gas, reducing the load on subsequent conversion processes. The heat required for the entire reaction can be provided by by-product pyrolysis semi-coke combustion. The invention avoids the problem that the combustion of the fuel in the conventional process provides heat and simultaneously burns the volatile matter, so that the content of H ₂ and CH ₄ in the pyrolysis gas is low, and the amount of reforming reaction of the subsequent gas composition is large. DRAWINGS

Figure 1 is a schematic view of a pyrolysis gasification apparatus of the present invention

2 is a schematic view of a pyrolysis gasification device combined with a two-stage rotary kiln according to the present invention;

3 is a schematic view of a pyrolysis gasification device using a hot flue gas as a heat source in combination with a two-stage rotary kiln according to the present invention; FIG. 4 is a schematic view of a pyrolysis gasification device combining a fluidized bed and a rotary kiln according to the present invention;

Figure 5 is a schematic view of a pyrolysis gasification device combining a fluidized bed and a plurality of rotary kiln according to the present invention;

Figure 6 is a schematic view of a pyrolysis gasification device combining a lean phase conveying bed and a rotary kiln according to the present invention;

7 is a schematic view of a pyrolysis gasification device combining a fluidized bed and a dilute phase transport bed according to the present invention;

Figure 8 is a schematic view of a pyrolysis gasification device combining a fluidized bed and a settling furnace according to the present invention;

Reference numeral

(1) Feeding device 2. Upstream pyrolysis reactor 3. Irrigation pipe 4. Downstream tar cracking reactor 5. Cyclone separator 6. Material leg

7. Exhaust pipe 8. Quenching device 9. Burner

10, fluidized bed 11, dilute phase transport bed 12, settling furnace

13. First rotary kiln reactor 14. Second rotary kiln reactor

The present invention will be further described below in conjunction with the accompanying drawings and embodiments.

1) feeding the carbonaceous solid raw material into the upstream pyrolysis reactor through a feeding device for pyrolysis to generate a pyrolysis gas phase product and a solid product;

2) The pyrolysis gas phase product and the solid product produced in the step 1) are passed into a downstream tar cracking reactor, and the tar is removed by high temperature thermal cracking, partial oxidation and pyrolysis semi-coke catalytic cracking reaction to obtain pyrolysis gas and pyrolysis half. focal.

The upstream pyrolysis reactor can be a rotary kiln, a fluidized bed or a dilute phase transport bed. The downstream tar cracking reactor described above may be a rotary kiln, a dilute phase transport bed, a settling furnace or a fixed bed.

The carbonaceous solid raw material is coal, biomass or other carbonaceous solid waste.

The reaction temperature in the upstream pyrolysis reactor is 700-100 CTC, and the reaction temperature in the downstream tar cracking reactor is 900-1300 °C.

Further preferably, the pyrolysis gas obtained in the step 2) is subjected to gas-solid separation; the pyrolysis semi-coke obtained in the step 2) is subjected to dry quenching, and waste heat recovery is performed. The pyrolysis gasification apparatus of the present invention based on the above-described pyrolysis gasification method for preparing a tar-free hydrogen-rich gas, as shown in FIG. 1, includes a feeding device 1, an overflow pipe 3, and an upstream pyrolysis reactor 2 and The downstream tar cracking reactor 4, which is in communication via an overflow pipe 3, is in communication with the upstream pyrolysis reactor 2.

The upstream pyrolysis reactor is preferably a rotary kiln, a fluidized bed or a dilute phase transport bed; the downstream tar cracking reactor is preferably a rotary kiln, a dilute phase transport bed, a settling furnace or a fixed bed.

The carbonaceous solid fuel is fed into the upstream pyrolysis reactor 2 via the feed device 1 for pyrolysis. The resulting pyrolysis semi-coke along with the pyrolysis gas phase product passes through the overflow pipe 3 and enters the downstream tar cracking reactor 4. In the downstream tar cracking reactor 4, the pyrolysis tar is pyrolyzed at a high temperature, partially oxidized and pyrolyzed. The semi-coke catalytic cracking is combined to remove a large amount of high-quality pyrolysis gas.

Preferably, the pyrolysis gasification device may further include a cyclone separator 5, a material leg 6, a discharge tube 7 and a quenching device 8, respectively, and the downstream tar cracking reactor 4 and the quenching device 8 In communication, the upper material inlet of the cyclone separator 5 is in communication with the quenching device 8 via a conduit, and the solid product outlet at the bottom of the cyclone separator 5 is in communication with the solid product collection device via the material leg 6.

The carbonaceous solid fuel is fed into the upstream pyrolysis reactor 2 via the feed device 1 for pyrolysis. The resulting pyrolysis semi-coke along with the pyrolysis gas phase product passes through the overflow pipe 3 and enters the downstream tar cracking reactor 4. In the downstream tar cracking reactor 4, the pyrolysis tar is pyrolyzed at a high temperature, partially oxidized and pyrolyzed. The semi-coke catalytic cracking is combined to remove a large amount of high-quality pyrolysis gas. The generated gas is subjected to gas-solid separation by the cyclone separator 5, and the resulting semi-focus is discharged to the quenching device 8 through the defocused tube 7 to perform quenching treatment.

Further, on the basis of the above-mentioned cyclone separator 5, the material leg 6, the defocusing tube 7 and the quenching device 8, the cyclone separator 5, the material leg 6, and the quenching device 8 may be further included. The upper material inlet of the cyclone separator 5 is in communication with the downstream tar cracking reactor 4 via a conduit, and the solid product outlet at the bottom of the cyclone separator 5 is in communication with the quenching device 8 via the feed leg 6.

The carbonaceous solid fuel is fed into the upstream pyrolysis reactor 2 via the feed device 1 for pyrolysis. The pyrolysis semi-coke passes through the overflow pipe 3 along with the pyrolysis gas phase product, and enters the downstream tar cracking reactor 4 for reaction. The resulting gas-solid mixture enters the cyclone separator 5 for gas-solid separation, and the resulting pyrolysis half-coke enters the quenching device 8 for quenching treatment.

Example 1

The schematic diagram of the pyrolysis gasification device combined with the two-stage rotary kiln reactor of the present embodiment is as shown in FIG. 2, and includes a feeding device 1, a first rotary kiln reactor 13, a second rotary kiln reactor 14, and a quenching device. 8. Cyclone separator 5 and material leg 6 etc. When the tar-free hydrogen-rich gas is prepared by using the pyrolysis gasification device, a carbonaceous solid fuel (for example, coal) having a particle size of <20 mm is sent to the upstream first rotary kiln via a feeding device 1 (such as a screw feeder). The reactor 13 is subjected to pyrolysis at 700-90 CTC, and the resulting mixed gas and solid product are passed through the overflow pipe 3 to the downstream second rotary kiln reactor 14. A certain amount of oxygen, water vapor or the like is introduced into the second rotary kiln reactor 14 and maintained at 110 CTC. In the second rotary kiln reactor 14, thermal cracking of the pyrolysis tar, partial oxidation, and catalytic cracking of the semi-coke on the pyrolysis tar are mainly caused to remove the tar; at the same time, partial gasification of the pyrolysis coke occurs, thereby obtaining a large amount High quality pyrolysis gases. The reacted product gas and pyrolysis half coke enter the quenching device 8 through the discharge tube 7, and the resulting semi-coke is subjected to quenching treatment and can be used for industrial production. The gasification gas obtained by gas-solid separation of the product gas through the cyclone separator 5 is used for industrial production and civil use. The solid product separated by cyclone 5 enters the solid product collection unit through feed leg 6.

The Xilinhot coal with a particle size of less than 5 mm was used as a raw material, and the experimental treatment capacity was 50 kg/h. The gas was H ₂ /CO=2.3 and the tar content was 30 mg/Nm ³ . Gas calorific value reaches 2300kcal / Nm

Example 2

A schematic diagram of the pyrolysis gasification apparatus of the present embodiment is shown in FIG. 3. In this embodiment, a burner 9 is additionally provided outside the first rotary kiln reactor 13 in the first embodiment, with hot flue gas as the first The heat source of the rotary kiln reactor 13 is the same as in the first embodiment.

Example 3

A schematic diagram of a pyrolysis gasification apparatus combining the fluidized bed of the present embodiment and a rotary kiln reactor is shown in FIG. 4, and includes a feeding device 1, a fluidized bed 10, a second rotary kiln reactor 14, and a quenching device 8. , cyclone separator 5 and material leg 6 and the like.

When the tar-free hydrogen-rich gas is prepared by using the pyrolysis gasification device, the carbonaceous solid fuel having a particle size of <20 mm is sent to the fluidized bed reactor 10 through the feeding device 1 for pyrolysis at 700-100 CTC, and is produced. The mixed gas and the solid product enter the downstream second rotary kiln reactor 14 via the overflow pipe 3. A certain amount of oxygen, water vapor or the like is introduced into the second rotary kiln reactor 14 and maintained at 1300 °C. In the second rotary kiln reactor 14, thermal cracking of the pyrolysis tar, partial oxidation, and catalytic cracking of the semi-coke on the pyrolysis tar are mainly caused to remove the tar; at the same time, partial gasification of the pyrolysis coke occurs, thereby obtaining a large amount High quality pyrolysis gases. The reacted product gas and pyrolysis half coke enter the quenching device 8 through the discharge tube 7, and the resulting semi-coke is subjected to quenching treatment and can be used for industrial production. The gasification gas obtained by gas-solid separation of the product gas through the cyclone separator 5 is used for industrial production and civil use. The solid product separated by cyclone 5 enters the solid product collection unit through feed leg 6. Example 4

The schematic diagram of the pyrolysis gasification device of the fluidized bed of the present embodiment combined with a plurality of rotary kiln reactors is shown in FIG. 5, including the feeding device 1, the fluidized bed 10, the second rotary kiln reactor 14, and the extinguishing device. The coke device 8, the cyclone separator 5 and the material leg 6. The process of specifically treating the reaction material is similar to that of the embodiment 3 except that a plurality of second rotary kiln reactors 14 are connected to the fluidized bed 10 to form a device group, which increases the throughput and improves the treatment efficiency.

Example 5

A schematic diagram of a pyrolysis gasification device combining the dilute phase transport bed and the rotary kiln reactor of the present embodiment is shown in FIG. 6, and includes a feeding device 1, a dilute phase transport bed 11, a second rotary kiln reactor 14, and a quenching unit. The coke device 8, the cyclone separator 5, the material leg 6, and the like.

When the tar-free hydrogen-rich gas is prepared by using the pyrolysis gasification device, several feeding devices 1 of the carbonaceous solid fuel having a particle size of <5 mm are sent to the dilute phase conveying bed 11 for pyrolysis at 700-90 CTC, resulting in pyrolysis. The mixed gas and the solid product enter the downstream second rotary kiln reactor 14 via the overflow pipe 3. A certain amount of oxygen, water vapor or the like is introduced into the second rotary kiln reactor 14 and maintained at 1100 °C. In the second rotary kiln reactor 14, thermal cracking of the pyrolysis tar, partial oxidation, and catalytic cracking of the semi-coke on the pyrolysis tar are mainly caused to remove the tar; at the same time, partial gasification of the pyrolysis coke occurs, thereby obtaining a large amount High quality pyrolysis gases. The reacted product gas and pyrolysis half coke enter the quenching device 8 through the discharge tube 7, and the resulting semi-coke is subjected to quenching treatment and can be used for industrial production. The gasification gas obtained by gas-solid separation of the product gas through the cyclone separator 5 is used for industrial production and civil use. The solid product separated by cyclone 5 enters the solid product collection unit through feed leg 6.

Example 6

A schematic diagram of a pyrolysis gasification device combining the fluidized bed and the dilute phase transport bed of the present embodiment is shown in FIG. 7, and includes a feeding device 1, a fluidized bed 10, a dilute phase transport bed 11, a quenching device 8, and a cyclone. Separator 5 and material leg 6 and the like.

When the tar-free hydrogen-rich gas is prepared by using the pyrolysis gasification device, the carbonaceous solid fuel having a particle size of <20 mm is fed into the fluidized bed 10 through the feeding device 1 and pyrolyzed at 700-90 CTC. The mixed gas and the solid product enter the dilute phase transport bed 11 through the overflow pipe 3. A certain amount of oxygen, water vapor or the like is introduced into the dilute phase transport bed 11 and maintained at 1100 °C. In the dilute phase transport bed 11, thermal cracking of the pyrolysis tar, partial oxidation, and catalytic cracking of the semi-coke on the pyrolysis tar are mainly caused to remove the tar; at the same time, partial gasification of the pyrolysis coke occurs, thereby obtaining a large amount of high quality. Pyrolysis gas. The gasification gas and pyrolysis semi-coke obtained after gas-solid separation of the product gas and pyrolysis semi-coke through the cyclone separator 5 can be used for Industrial production and civil use. The solid product separated by the cyclone separator 5 enters the quenching device 8 through the material leg 6, and is subjected to quenching treatment to be used for industrial production.

The Xilinhot coal with a particle size of 0.5-1.5 mm was used as a raw material, and the experimental treatment capacity was 50 kg/h. The gas was H ₂ /CO=2 and the tar content was 50 mg/Nm ³ . Gas calorific value reaches 1500kcal/Nm

Example 7

The schematic diagram of the pyrolysis gasification device combined with the fluidized bed and the settling furnace reactor of the present embodiment is shown in Fig. 8, including the feeding device 1, the fluidized bed 10, the settling furnace 12, the quenching device 8, and the cyclone separation. 5 and the leg 6 and the like.

When the tar-free hydrogen-rich gas is prepared by using the pyrolysis gasification device, the carbonaceous solid fuel having a particle size of <20 mm is sent to the fluidized bed 10 through the screw feeder 1 to be pyrolyzed at 700-90 CTC, and the resulting mixture is mixed. The gas as well as the solid product enters the settling furnace 12 via the overflow pipe 3. A certain amount of oxygen, water vapor or the like is introduced into the settling furnace 12 and maintained at 1100 °C. In the settling furnace 12, thermal cracking of the pyrolysis tar, partial oxidation, and catalytic cracking of the semi-coke on the pyrolysis tar are mainly caused to remove the tar; at the same time, partial gasification of the pyrolysis coke occurs, thereby obtaining a large amount of high-quality pyrolysis. gas. The pyrolysis semi-coke after the reaction is directly introduced into the quenching device 8 by the settling furnace 12, and the resulting semi-coke is subjected to quenching treatment and can be used for industrial production. The gas of the product gas obtained by gas-solid separation by cyclone separator 5 is used for industrial production and civil use. The solid product separated by the cyclone separator 5 enters the quenching device 8 through the material leg 6, and is quenched and processed for industrial production.

It should be noted that, for the specific implementation method of the present invention, such as different tissue forms of the reactor, the reaction atmosphere and the like can be improved according to specific practical needs; the entire reaction device can be carried out under normal pressure or under pressurized conditions. The reaction raw material may be added with a certain amount of calcium-based minerals or other minerals or catalysts having tar cracking ability, all of which do not contradict the main idea of the present invention.

Claims

Rights request

1. A pyrolysis gasification method for preparing tar-free hydrogen-rich gas, including the following steps:

1) Send the carbonaceous solid raw materials into the upstream pyrolysis reactor through the feeding device for aerobic pyrolysis to produce pyrolysis gas phase products and solid products;

2) Pass the pyrolysis gas phase products and solid products produced in step 1) into the downstream tar cracking reactor, and remove the tar through high-temperature thermal cracking, partial oxidation and pyrolysis semi-coke catalytic cracking reactions; at the same time, pyrolysis semi-coke generates part of the gas to obtain pyrolysis gas and pyrolysis semi-coke.

2. The pyrolysis gasification method according to claim 1, characterized in that the carbon-containing solid raw material is coal, biomass or carbon-containing solid waste.

3. The pyrolysis gasification method according to claim 1, characterized in that the reaction temperature in the upstream pyrolysis reactor is 700-1000°C, and the reaction temperature in the downstream tar cracking reactor is 900-1300°C. °C.

4. The pyrolysis gasification method according to claims 1-3, characterized in that gas-solid separation is performed on the pyrolysis product obtained in step 2); pyrolysis gas and pyrolysis semi-coke products are obtained.

5. The pyrolysis gasification method according to claims 1-3, characterized in that a certain amount of calcium-based minerals or other catalysts with tar cracking capabilities can be added to the pyrolysis raw materials.

6. A pyrolysis gasification device based on the pyrolysis gasification method for preparing tar-free hydrogen-rich gas according to claim 1, including a feeding device (1), an overflow pipe (3), an upstream pyrolysis reactor ( 2), the feeding device

(1) is connected to the upstream pyrolysis reactor (2), and is characterized in that it also includes a downstream tar cracking reactor (4), which is connected to the upstream pyrolysis reactor (2) through an overflow pipe (3).

7. The pyrolysis gasification device according to claim 6, characterized in that the upstream pyrolysis reactor is a rotary kiln, a fluidized bed or a dilute phase transport bed.

8. The pyrolysis gasification device according to claim 6 or 7, characterized in that the downstream tar cracking reactor is a rotary kiln, a dilute phase transport bed, a settling furnace or a fixed bed.

9. The pyrolysis gasification device according to claim 6, further comprising a cyclone separator (5), a material leg (6), a coke discharge pipe (7) and a coke quenching device (8), The coke discharge pipe (7) is connected to the downstream tar cracking reactor (4) and the coke quenching device (8) respectively. The upper material inlet of the cyclone separator (5) is connected to the coke quenching device (8) through a pipeline. The cyclone The solid product outlet at the bottom of the separator (5) is connected to the solid product collection device through the material leg (6).

10. The pyrolysis gasification device according to claim 6, further comprising a cyclone separator

(5), material leg (6), and coke quenching device (8), the upper material inlet of the cyclone separator (5) passes through the tube The channel is connected to the downstream tar cracking reactor (4), and the solid product outlet at the bottom of the cyclone separator (5) is connected to the coke quenching device (8) through the material leg (6).