Biomass drum carbonization poly-generation coupled steam gasification hydrogen production device and method

Abstract

Biomass drum carbonization poly-generation coupled steam gasification hydrogen production device and method, belonging to the fields of chemical engineering and power generation. The gas outlet of the drum carbonizer is connected to the gas burner through an air-tar cooler, a multi-stage indirect water-cooled wood vinegar liquid cooler, and a wood vinegar liquid spray tower. The high-temperature flue gas outlet of the furnace is connected to the circulating fluidized bed. The circulating fluidized bed is connected to a high-efficiency cyclone separator I. The ash discharge port of the high-efficiency cyclone separator I is connected to the ash inlet of the differential fluidized bed gasifier. The biomass carbon outlet of the drum carbonizer is connected to the feed inlet of the differential fluidized bed gasifier. The ash discharge port of the differential fluidized bed gasifier is connected to the lower part of the circulating fluidized bed. The differential fluidized bed gasifier is sequentially connected to a high-efficiency cyclone separator II, a superheater, an air preheater III, a dust collector, a high-temperature steam conversion reactor, an air preheater II, a low-temperature steam conversion reactor, an air preheater I, a condenser, an organic amine scrubber, a compressor, and a pressure swing adsorption system. The present invention is used for biomass gasification hydrogen production.

Description

Technical Field

[0001] The invention belongs to the technical fields of chemical industry and power generation, and particularly relates to a biomass drum carbonization polygeneration coupling steam gasification hydrogen production device and method. Background Art

[0002] The products produced by biomass drum carbonization "polygeneration" are biomass charcoal, tar and wood vinegar liquid. When using wood or bamboo as the carbonization raw material, the biomass charcoal can be used as the raw material for producing "activated carbon" or "machine-made charcoal", the biomass tar can be used as liquid fuel or chemical raw material, and the wood vinegar liquid can be used as foliar fertilizer or pesticide, realizing the high-value utilization of biomass. However, when using agricultural straw as the carbonization raw material to produce biomass charcoal, due to the presence of alkali metals K and Na and relatively low calorific value (≤5000Kcal / kg), it can generally only be used for soil improvement or production of carbon-based compound fertilizers, with low economic benefits, resulting in the stagnation of this industry. The invention proposes a biomass drum carbonization "polygeneration" coupling steam gasification hydrogen production process to solve the problem of high-value utilization of biomass charcoal. Summary of the Invention

[0003] The purpose of the invention is to solve the problem of high-value utilization of biomass charcoal in the biomass drum carbonization process, and propose a biomass drum carbonization polygeneration coupling steam gasification hydrogen production device and method.

[0004] The invention uses the high-temperature circulating ash of a circulating fluidized bed as the heat source and high-temperature steam as the gasification medium to gasify biomass charcoal in a differential fluidized bed to produce hydrogen, realizing the high-value utilization of biomass charcoal.

[0005] To achieve the above purpose, the technical solutions adopted by the invention are as follows:

[0006] Solution 1: A biomass drum carbonization polygeneration coupling steam gasification hydrogen production device, comprising a screw feeder 1, a drum carbonizer, a gas burner, a screw feeder 2, an air-tar cooler, a multi-stage indirect water-cooled wood vinegar liquid cooler, a gas blower, a wood vinegar liquid spray tower, a screw feeder 3, a screw feeder 4, a circulating fluidized bed, a high-efficiency cyclone separator 1, a high-efficiency cyclone separator 2, a differential fluidized bed gasification furnace, a waste heat boiler, a back-pressure steam turbine generator set, a superheater, an air preheater 3, a dust collector, a high-temperature steam conversion reactor, an air preheater 2, a low-temperature steam conversion reactor, an air preheater 1, a condenser, an organic amine scrubber, a compressor and a pressure swing adsorption system;

[0007] The first screw feeder is a biomass screw feeder, the third screw feeder is an auxiliary fuel feeder, and the fourth screw feeder is a circulating material feeder. The circulating material consists of limestone and dolomite. The discharge port of the first screw feeder is connected to the feed port at one end of the drum carbonizer. The discharge port at the other end of the drum carbonizer is connected to the biomass carbon inlet of the differential fluidized bed gasifier through the second screw feeder. The pyrolysis gas outlet of the drum carbonizer is connected to the pyrolysis gas inlet of the air-tar cooler. The air outlet of the air-tar cooler is connected to the air inlet of the gas burner through a pipeline. The pyrolysis gas outlet of the air-tar cooler is sequentially connected to the multi-stage indirect water-cooled wood vinegar liquid cooler, the gas blower, and the pyrolysis gas inlet of the wood vinegar liquid spray tower. The pyrolysis gas outlet of the wood vinegar liquid spray tower is connected to the pyrolysis gas inlet of the gas burner through a pipeline. The outlet of the gas burner is connected to the furnace chamber of the drum carbonizer. The flue gas outlet at the top of the drum carbonizer is connected to the flue gas inlet of the circulating fluidized bed. The circulating fluidized bed is an adiabatic combustion chamber. The discharge ports of the third and fourth screw feeders are connected to the circulating fluidized bed. The flue gas outlet at the top of the circulating fluidized bed is connected to the flue gas inlet of the first high-efficiency cyclone separator. The discharge port at the lower end of the first high-efficiency cyclone separator is connected to the first feed port of the differential fluidized bed gasifier through the first return valve. The discharge port of the differential fluidized bed gasifier is connected to the return feed inlet of the circulating fluidized bed through the second return valve. The flue gas outlet at the top of the first high-efficiency cyclone separator is connected to the flue gas inlet of the waste heat boiler. The steam outlet of the waste heat boiler is connected to the steam inlet of the back-pressure steam turbine generator set. The exhaust port of the back-pressure steam turbine generator set is connected to the steam inlet of the superheater. The superheated steam outlet of the superheater is connected to the superheated steam inlet at the bottom of the differential fluidized bed gasifier. The syngas outlet at the top of the differential fluidized bed gasifier is connected to the syngas inlet of the second high-efficiency cyclone separator. The syngas outlet at the top of the second high-efficiency cyclone separator is connected to the syngas inlet of the superheater. The syngas outlet of the superheater is sequentially connected to the third air preheater, the dust collector, the high-temperature steam reforming reactor, the second air preheater, the low-temperature steam reforming reactor, the first air preheater, the condenser, the organic amine scrubber, the compressor, and the pressure swing adsorption system. The exhaust port of the pressure swing adsorption system is connected to the intake port at the lower part of the circulating fluidized bed through a pipeline. The discharge port at the lower part of the second high-efficiency cyclone separator is connected to the second feed port at the lower part of the differential fluidized bed gasifier.

[0008] Furthermore, the feed water outlet of the waste heat boiler is connected to the feed water inlet of the waste heat boiler through the condenser.

[0009] A method for hydrogen production by coupling biomass drum carbonization and steam gasification in a polygeneration system, the method comprising the following steps:

[0010] Step 1: The first screw feeder feeds biomass into the drum carbonizer for dry distillation. The biomass charcoal discharged from the drum carbonizer is sent into the differential fluidized bed gasifier through the second screw feeder. There is at least 1 drum carbonizer, and multiple ones can operate simultaneously as needed. Under steam as the gasifying agent, hydrogen-rich syngas is produced. The pyrolysis gas generated by the drum carbonizer first enters the air-tar cooler. After the air is preheated, it is sent into the gas burner to be mixed with the pyrolysis gas and then sent into the furnace of the drum carbonizer for combustion and heat release. Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar liquid cooler and the gas blower to send the pyrolysis gas into the wood vinegar liquid spray tower, and then into the gas burner and sprayed into the furnace of the drum carbonizer for combustion. The high-temperature flue gas at 800 - 850 °C is discharged from the flue gas outlet at the top of the drum carbonizer and enters the furnace of the circulating fluidized bed. The third screw feeder feeds biomass into the circulating fluidized bed for combustion, and at the same time, the fourth screw feeder feeds the circulating material into the circulating fluidized bed for calcination;

[0011] The high-temperature air at 400 - 450 °C enters the circulating fluidized bed from the bottom air chamber of the circulating fluidized bed to assist combustion. The high-temperature flue gas at 900 - 950 °C carrying the circulating material comes out from the flue gas outlet at the top of the circulating fluidized bed and enters the first high-efficiency cyclone separator to separate the circulating material, and then is sent into the differential fluidized bed gasifier through the first return valve. At the same time, the biomass charcoal discharged from the drum carbonizer is sent into the differential fluidized bed gasifier through the second screw feeder and reacts with the high-temperature steam at 550 - 600 °C to generate syngas at a bed temperature of 780 - 850 °C;

[0012] Step 2: The high-temperature flue gas coming out from the flue gas outlet at the top of the first high-efficiency cyclone separator enters the waste heat boiler. The steam generated by the waste heat boiler is sent to the back-pressure steam turbine generator set for power generation. The steam discharged from the back-pressure steam turbine generator set enters the superheater and is heated to 550 - 600 °C and then enters the differential fluidized bed gasifier from the bottom of the differential fluidized bed gasifier;

[0013] Step 3: In the differential fluidized bed gasifier, the high-temperature circulating material and the high-temperature superheated steam heat the differential fluidized bed gasifier to 780 - 850 °C. The biomass charcoal reacts with the high-temperature steam at this temperature to generate syngas H2, CO, CO2, CH4 and trace H2S. The mass ratio of steam to biomass charcoal = 1 - 3:1, and the gas production rate of biomass charcoal is 2.5 - 3.0 Nm 3 / kg; At the same time, CaO and MgO formed after the calcination of limestone and dolomite react with H2S to remove 90% of H2S, and H2S < 10 mg / Nm 3 ;

[0014] Step 4: The high-temperature syngas coming out from the top of the differential fluidized bed gasifier enters the high-efficiency cyclone separator II, where the circulating materials carried therein are separated and returned to the differential fluidized bed gasifier. Then the syngas passes through the superheater and the air preheater III and is cooled to 350°C, and then enters the dust collector. After dust removal, the syngas enters the high-temperature water vapor shift reactor, and the temperature rises to 380 - 450°C and enters the air preheater II, where the air is preheated to 250 - 300°C. The temperature of the syngas drops to 190 - 200°C and then enters the low-temperature water vapor shift reactor, with a steam / CO molar ratio ≥ 2. The total conversion rate of CO in the high-temperature and low-temperature water gas shift reactions: CO + H2O = H2 + CO2 is over 95%; the syngas is heated to 250 - 260°C, and then enters the air preheater I, where the air is preheated from room temperature to 130 - 150°C, and the temperature of the syngas drops to 120 - 150°C. Then the syngas enters the condenser, and the water vapor in the syngas is condensed using the feed water of the waste heat boiler; then the syngas enters the organic amine scrubber to remove the remaining dust, trace H2S and over 90% of CO2 in the syngas. The clean syngas is cooled to 50 - 60°C, and the organic amine aqueous solution is regenerated after absorbing CO2; then the syngas enters the pressure swing adsorption system through a compressor to obtain 99.9% H2, and the exhaust gas from the pressure swing adsorption system is sent to the circulating fluidized bed for combustion to release heat.

[0015] Scheme 2: A biomass drum carbonization polygeneration coupled with steam gasification hydrogen production device, including a screw feeder I, a drum carbonizer, a gas burner, a screw feeder II, an air-tar cooler, a multi-stage indirect water-cooled wood vinegar cooler, a gas blower, a wood vinegar spray tower, a screw feeder III, a screw feeder IV, a circulating fluidized bed, a high-efficiency cyclone separator I, a high-efficiency cyclone separator II, a differential fluidized bed gasifier, a waste heat boiler, a back-pressure steam turbine generator set, a superheater, an air preheater III, a dust collector, a high-temperature water vapor shift reactor, an air preheater II, a low-temperature water vapor shift reactor, an air preheater I, a condenser, an organic amine scrubber, a compressor and a pressure swing adsorption system;

[0016] The first screw feeder is a biomass screw feeder, the third screw feeder is a biomass feeder, and the fourth screw feeder is a circulating material feeder; the discharge port of the screw feeder is communicated with the feed port at one end of the drum carbonizer, and the discharge port at the other end of the drum carbonizer is communicated with the biomass carbon inlet of the differential fluidized bed gasifier through the second screw feeder; the pyrolysis gas outlet of the drum carbonizer is communicated with the pyrolysis gas inlet of the air-tar cooler, the air outlet of the air-tar cooler is communicated with the air inlet of the gas burner through a pipeline, the pyrolysis gas outlet of the air-tar cooler is successively communicated with the multi-stage indirect water-cooled wood vinegar liquid cooler, the gas blower and the pyrolysis gas inlet of the wood vinegar liquid spray tower, the pyrolysis gas outlet of the wood vinegar liquid spray tower is communicated with the pyrolysis gas inlet of the gas burner through a pipeline, and the outlet of the gas burner is communicated with the furnace chamber of the drum carbonizer; the flue gas outlet at the top of the drum carbonizer is communicated with the flue gas inlet of the circulating fluidized bed, the circulating fluidized bed is an adiabatic combustion chamber, the discharge ports of the third and fourth screw feeders are communicated with the circulating fluidized bed, the flue gas outlet at the top of the circulating fluidized bed is communicated with the flue gas inlet of the first high-efficiency cyclone separator, the discharge port at the lower end of the first high-efficiency cyclone separator is respectively communicated with the first feed port of the differential fluidized bed gasifier and the return port of the circulating fluidized bed through the first return valve, and the discharge port of the differential fluidized bed gasifier is communicated with the return inlet of the circulating fluidized bed through the second return valve; the flue gas outlet at the top of the first high-efficiency cyclone separator is communicated with the flue gas inlet of the waste heat boiler, the steam outlet of the waste heat boiler is communicated with the steam inlet of the back-pressure steam turbine generator set, the exhaust port of the back-pressure steam turbine generator set is communicated with the steam inlet of the superheater, and the superheated steam outlet of the superheater is communicated with the superheated steam inlet at the bottom of the differential fluidized bed gasifier; the syngas outlet at the top of the differential fluidized bed gasifier is communicated with the syngas inlet of the second high-efficiency cyclone separator, the syngas outlet at the top of the second high-efficiency cyclone separator is communicated with the syngas inlet of the superheater, and the syngas outlet of the superheater is successively communicated with the third air preheater, the dust collector, the high-temperature water vapor conversion reactor, the second air preheater, the low-temperature water vapor conversion reactor, the first air preheater, the condenser, the organic amine scrubber, the compressor and the pressure swing adsorption system, and the exhaust port of the pressure swing adsorption system is communicated with the air inlet at the lower part of the circulating fluidized bed through a pipeline; the discharge port at the lower part of the second high-efficiency cyclone separator is communicated with the second feed port at the lower part of the differential fluidized bed gasifier.

[0017] Further, the feed water outlet of the waste heat boiler is communicated with the feed water inlet of the waste heat boiler through the condenser.

[0018] A method for hydrogen production by coupling biomass drum carbonization and steam gasification in a polygeneration system, the method comprising the following steps:

[0019] Step 1: The first screw feeder feeds biomass into the drum carbonizer for dry distillation. The biomass charcoal discharged from the drum carbonizer is sent into the differential fluidized bed gasifier through the second screw feeder, and hydrogen-rich syngas is produced with steam as the gasifying agent. The pyrolysis gas generated by the drum carbonizer first enters the air-tar cooler. After the air is preheated, it is sent into the gas burner to be mixed with the pyrolysis gas and then sent into the furnace of the drum carbonizer for combustion and heat release. Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar liquid cooler and the gas blower to send the pyrolysis gas into the wood vinegar liquid spray tower, and then into the gas burner and sprayed into the furnace of the drum carbonizer for combustion. The high-temperature flue gas at 800 - 850 °C is discharged from the flue gas outlet at the top of the drum carbonizer and enters the furnace of the circulating fluidized bed. The third screw feeder feeds the auxiliary fuel biomass into the circulating fluidized bed for combustion, and at the same time, the fourth screw feeder feeds the circulating material into the circulating fluidized bed for calcination;

[0020] The high-temperature air at 300 - 350 °C enters the circulating fluidized bed from the bottom air chamber of the circulating fluidized bed for combustion support. The high-temperature flue gas at 900 - 950 °C carrying the circulating material comes out from the flue gas outlet at the top of the circulating fluidized bed and enters the high-efficiency cyclone separator I to separate the circulating material. Part of it is sent back into the circulating fluidized bed through the return valve I, and the other part is sent into the differential fluidized bed gasifier through the return valve I;

[0021] Step 2: The high-temperature flue gas coming out from the flue gas outlet at the top of the high-efficiency cyclone separator I enters the waste heat boiler. The steam generated by the waste heat boiler is sent to the back-pressure steam turbine generator set for power generation. The steam discharged from the back-pressure steam turbine generator set enters the superheater and is heated to 400 - 450 °C, and then enters the differential fluidized bed gasifier from the bottom of the differential fluidized bed gasifier;

[0022] Step 3: In the differential fluidized bed gasifier, the high-temperature circulating material and the high-temperature superheated steam heat the differential fluidized bed gasifier to 600 - 700 °C. The biomass charcoal discharged from the drum carbonizer is sent into the differential fluidized bed gasifier through the second screw feeder. The mass ratio of steam to biomass charcoal = 1 - 3:1. The biomass charcoal reacts with the high-temperature steam under the action of a catalyst to generate syngas H2, CO, CO2, CH4, and H2S. The gas production rate of biomass charcoal is 2.0 - 2.5 Nm 3 / kg; CaO undergoes an in-situ absorption reaction with CO2 to form CaCO3, promoting the forward progress of CO + H2O = H2 + CO2. At the same time, CaO reacts with H2S to form CaS, removing 90% of H2S, so that H2S in the syngas < 10 mg / Nm 3The circulating materials containing CaCO3 and CaS and the unreacted biochar enter the circulating fluidized bed through the second return valve, causing the decomposition of CaCO3 into CaO and CO2, and the decomposition of CaS into CaO and SO2. After the Ni-based catalyst eliminates carbon deposition in the circulating fluidized bed, it enters the differential fluidized bed gasifier together with CaO and MgO after being separated by the first high-efficiency cyclone separator;

[0023] Step 4: The syngas at 600 - 700 °C coming out from the top of the differential fluidized bed gasifier first enters the second high-efficiency cyclone separator to separate the circulating materials carried therein and return them to the differential fluidized bed gasifier. The syngas coming out from the top of the second high-efficiency cyclone separator enters the superheater and the third air preheater, and its temperature drops to 350 °C. Then it enters the dust collector. After dust removal, the syngas enters the high-temperature steam shift reactor, and its temperature rises to 380 - 450 °C and enters the second air preheater to preheat the air to 250 - 300 °C. After the temperature of the syngas drops to 190 - 200 °C, it enters the low-temperature steam shift reactor with a steam / CO molar ratio ≥ 2. After the high- and low-temperature water-gas shift reactions: CO + H2O = H2 + CO2, the total conversion rate of CO is over 95%. The syngas temperature rises to 250 - 260 °C, and then enters the first air preheater to preheat the air from room temperature to 130 - 150 °C. The syngas temperature drops to 120 - 150 °C, and then the syngas enters the condenser, and the waste heat boiler feed water is used to condense the water vapor in the syngas. Then the syngas enters the organic amine scrubber to remove the remaining dust, trace H2S and over 90% of CO2 in the syngas. The clean syngas temperature drops to 50 - 60 °C, and the organic amine aqueous solution is regenerated after absorbing CO2. Then the syngas enters the pressure swing adsorption system through a compressor to obtain 99.9% H2, and the exhaust gas from the pressure swing adsorption system is sent to the circulating fluidized bed for combustion to release heat.

[0024] The beneficial effects of the present invention compared with the prior art are as follows: The present invention solves the problem of the outlet of biochar and converts biochar into H2, realizing the high-value utilization of biochar. The present invention uses the heat of high-temperature circulating ash at 900 - 950 °C, plus superheated steam at 550 - 600 °C as the fluidizing medium and reactant, ensuring that the temperature of the differential fluidized bed gasifier is within a reasonable temperature range and greatly reducing the equipment investment cost. The present invention has significant economic efficiency and innovation in coupling the power generation of a waste heat boiler with a back-pressure steam turbine generator set and the hydrogen production from biochar gasification. In addition, after using the high-temperature steam shift reactor (WSG-1) and the low-temperature steam shift reactor (WSG-2), the volume fraction of H2 can reach 85%. After absorbing CO2 by organic amine and pressure swing adsorption (PSA), 99.9% H2 is obtained. Brief Description of the Drawings

[0025] Figure 1 is the structural schematic diagram of the biomass drum carbonization polygeneration coupled steam gasification hydrogen production device of the present inventionFigure 1 The operating temperature of the differential fluidized bed gasifier is 780 - 850 °C;

[0026] Figure 2 is the structural schematic of the biomass drum carbonization polygeneration coupled steam gasification hydrogen production device of the present invention Figure 2 The operating temperature of the differential fluidized bed gasifier is 600 - 700 °C, with in-situ CO2 absorption;

[0027] Figure 3 is Figure 1 the partial enlarged view of part A of

[0028] Figure 4 is Figure 1 the partial enlarged view of part B of

[0029] Figure 5 is Figure 1 the partial enlarged view of part C of

[0030] Figure 6 is Figure 1 the partial enlarged view of part D of

[0031] Figure 7 is Figure 2 the partial enlarged view of part E of

[0032] Figure 8 is Figure 2 the partial enlarged view of part F of

[0033] The names of the components involved in the above drawings and the corresponding reference numerals are as follows:

[0034] Screw feeder 1, Drum carbonizer 2, Gas burner 3, Furnace 4 of drum carbonizer 2, Screw feeder 2 5, Blower 1 6, Air-tar cooler 7, Multi-stage indirect water-cooled wood vinegar liquid cooler 8, Gas blower 9, Wood vinegar liquid spray tower 10, Screw feeder 3 11-1, Screw feeder 4 11-2, Circulating fluidized bed 12, High-efficiency cyclone separator 1 13, High-efficiency cyclone separator 2 14, Return valve 1 15, Differential fluidized bed gasifier 16, Biomass charcoal inlet 17, Return valve 2 18, Waste heat boiler 19, Back-pressure steam turbine generator set 20, Induced draft fan 21, Chimney 22, Superheater 23, Air preheater 3 24, Dust collector 25, Ash bin 26, High-temperature steam reforming reactor 27, Air preheater 2 28, Low-temperature steam reforming reactor 29, Air preheater 1 30, Blower 2 31, Condenser 32, Organic amine scrubber 33, Compressor 34, Pressure swing adsorption system 35, Motor 36, Gear transmission mechanism 37. Detailed implementation manners

[0035] Detailed implementation manner one: As Figure 1 , Figures 3 - 6As shown in the figure, this embodiment discloses a biomass drum carbonization poly-generation coupled steam gasification hydrogen production device, including a screw feeder 1, a drum carbonizer 2, a gas burner 3, a screw feeder 5, an air-tar cooler 7, a multi-stage indirect water-cooled wood vinegar liquid cooler 8, a gas blower 9, a wood vinegar liquid spray tower 10, a screw feeder 11-1, a screw feeder 11-2, a circulating fluidized bed 12, a high-efficiency cyclone separator 13, a high-efficiency cyclone separator 14, a differential fluidized bed gasifier 16, a waste heat boiler 19, a back-pressure steam turbine generator set 20, a superheater 23, an air preheater 3 24, a dust collector 25, a high-temperature steam shift reactor 27, an air preheater 2 28, a low-temperature steam shift reactor 29, an air preheater 1 30, a condenser 32, an organic amine scrubber 33, a compressor 34, and a pressure swing adsorption system (PSA) 35;

[0036] The screw feeder 1 is a biomass screw feeder, the screw feeder 11-1 is an auxiliary fuel feeder (the auxiliary fuel is agricultural and forestry biomass), and the screw feeder 11-2 is a circulating material feeder; the circulating material is composed of limestone and dolomite, and the mass ratio of limestone to dolomite = 1:1; the discharge port of the screw feeder 1 is communicated with the feed port at one end of the drum carbonizer 2, and the discharge port at the other end of the drum carbonizer 2 is communicated with the biomass carbon inlet 17 of the differential fluidized bed gasifier 16 through the screw feeder 5;

[0037] The pyrolysis gas outlet of the drum carbonizer 2 is communicated with the pyrolysis gas inlet of the air-tar cooler 7, the air outlet of the air-tar cooler 7 is communicated with the air inlet of the gas burner 3 through a pipeline, the pyrolysis gas outlet of the air-tar cooler 7 is successively communicated with the multi-stage indirect water-cooled wood vinegar liquid cooler 8, the gas blower 9, and the pyrolysis gas inlet of the wood vinegar liquid spray tower 10, the pyrolysis gas outlet of the wood vinegar liquid spray tower 10 is communicated with the pyrolysis gas inlet of the gas burner 3 through a pipeline, and the outlet of the gas burner 3 is communicated with the furnace 4 (the furnace for burning biomass pyrolysis gas) of the drum carbonizer 2;

[0038] The flue gas outlet at the top of the drum carbonizer 2 is communicated with the flue gas inlet of the circulating fluidized bed 12. The circulating fluidized bed 12 is an adiabatic combustion chamber. The discharge ports of the screw feeder 11-1 and the screw feeder 11-2 are communicated with the circulating fluidized bed 12. The flue gas outlet at the top of the circulating fluidized bed 12 is communicated with the flue gas inlet of the high-efficiency cyclone separator 13. The discharge port at the lower end of the high-efficiency cyclone separator 13 is communicated with the first feed port of the differential fluidized bed gasifier 16 through a return valve 15. The discharge port of the differential fluidized bed gasifier 16 is communicated with the return feed inlet of the circulating fluidized bed 2 through a return valve 18;

[0039] The flue gas outlet at the top of the high-efficiency cyclone separator 13 is connected to the flue gas inlet of the waste heat boiler 19. The steam outlet of the waste heat boiler 19 is connected to the steam inlet of the back-pressure steam turbine generator set 20. The exhaust port of the back-pressure steam turbine generator set 20 is connected to the steam inlet of the superheater 23. The superheated steam outlet of the superheater 23 is connected to the superheated steam inlet at the bottom of the differential fluidized bed gasifier 16;

[0040] The syngas outlet at the top of the differential fluidized bed gasifier 16 is connected to the syngas inlet of the high-efficiency cyclone separator 14. The syngas outlet at the top of the high-efficiency cyclone separator 14 is connected to the syngas inlet of the superheater 23. The syngas outlet of the superheater 23 is successively connected to the air preheater 24, the dust collector 25, the high-temperature water vapor shift reactor 27, the air preheater 28, the low-temperature water vapor shift reactor 29, the air preheater 30, the condenser 32, the organic amine scrubber 33, the compressor 34, and the pressure swing adsorption system 35. The exhaust port of the pressure swing adsorption system 35 is connected to the air inlet at the lower part of the circulating fluidized bed 12 through a pipeline;

[0041] The discharge port at the lower part of the high-efficiency cyclone separator 14 is connected to the second feed port at the lower part of the differential fluidized bed gasifier 16.

[0042] Furthermore, the feed water outlet of the waste heat boiler 19 is connected to the feed water inlet of the waste heat boiler 19 through the condenser 32. The feed water of the waste heat boiler 19 is preheated by the condenser 32 and then enters the waste heat boiler 19 through the feed water inlet of the waste heat boiler 19.

[0043] Specific Embodiment 2: As Figure 1 、 Figures 3 - 6 shown (operating temperature of the differential fluidized bed gasifier: 780 - 850 °C), this embodiment discloses a method for biomass drum carbonization polygeneration coupled with steam gasification for hydrogen production. The method is implemented based on the device described in Specific Embodiment 1, and the method includes the following steps:

[0044] Step 1: The screw feeder 1 feeds biomass (biomass is agricultural and forestry waste, feeding rate: 1 - 5 t / h) into the drum carbonizer 2 for carbonization. The biomass charcoal discharged from the drum carbonizer 2 is sent into the differential fluidized bed gasifier 16 (there is a biomass charcoal inlet 17 on the differential fluidized bed gasifier 16) through the screw feeder 2. There is at least 1 drum carbonizer 2, and multiple ones can operate simultaneously as needed. Under steam as the gasifying agent, hydrogen-rich syngas is produced. The pyrolysis gas generated by the drum carbonizer 2 first enters the air-tar cooler 7 (to condense and recover tar as chemical raw materials). After the air is preheated, it is sent into the gas burner 3 to be mixed with the pyrolysis gas and then sent into the furnace 4 of the drum carbonizer 2 for combustion and heat release (providing the heat required for the drum carbonization of the drum carbonizer 2). Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar liquid cooler 8 (to condense and collect the wood vinegar liquid, and after vacuum extraction technology, the wood vinegar liquid is purified and used as foliar fertilizer and insecticide) and the gas blower 9 to send the pyrolysis gas into the wood vinegar liquid spray tower 10 (the purpose is to further reduce the tar content in the pyrolysis gas. The purified wood vinegar liquid is used as the spray liquid, so that the tar content in the pyrolysis gas is less than 50 mg / Nm 3 ), and then it is sent into the gas burner 3 and sprayed into the furnace 4 of the drum carbonizer 2 for combustion (the combustion temperature reaches 1100 - 1200 °C). The high-temperature flue gas at 800 - 850 °C is discharged from the flue gas outlet at the top of the drum carbonizer 2 and enters the furnace of the circulating fluidized bed 12. The screw feeder 3 11-1 feeds biomass (agricultural and forestry waste; (the biomass quantity meets the outlet temperature of the circulating fluidized bed 12 at 900 - 950 °C, and the feeding rate is determined by the load) into the circulating fluidized bed 12 for combustion. At the same time, the screw feeder 4 11-2 feeds the circulating material (the circulating material is composed of limestone and dolomite, and the mass ratio of limestone to dolomite = 1:1) into the circulating fluidized bed 12 for calcination (when starting up, the circulating material is gradually added until normal operation. During normal operation, it is supplemented according to the material loss of the system. The calcination product is used as bed material on the one hand and as a catalyst for the differential fluidized bed gasifier 16 on the other hand);

[0045] The high-temperature air at 400 - 450 °C enters the circulating fluidized bed 12 from the bottom air chamber of the circulating fluidized bed 12 to assist combustion (the circulating fluidized bed 12 is an adiabatic combustion furnace, the fluidization velocity is 6 - 10 m / s, and the circulation ratio is 30 - 100). The high-temperature flue gas at 900 - 950 °C coming out from the flue gas outlet at the top of the circulating fluidized bed 12 carries the circulating material (the calcination product of limestone and dolomite) into the high-efficiency cyclone separator 1. The circulating material is separated and sent into the differential fluidized bed gasifier 16 through the return valve 15. At the same time, the biomass charcoal discharged from the drum carbonizer 2 is sent into the differential fluidized bed gasifier 16 through the screw feeder 2 and reacts with the high-temperature steam at 550 - 600 °C sent in to generate syngas (main components: H2, CO, CO2, CH4) at a bed temperature of 780 - 850 °C;

[0046] Step 2: The high-temperature flue gas discharged from the flue gas outlet at the top of the high-efficiency cyclone separator 13 enters the waste heat boiler 19, and the steam generated by the waste heat boiler 19 is sent to the back-pressure steam turbine generator set 20 for power generation; the steam (with a pressure of 0.2 - 0.3 MPa and a temperature of 200 - 250 °C) discharged from the back-pressure steam turbine generator set 20 enters the superheater 23, is heated to 550 - 600 °C, and then enters the differential fluidized bed gasifier 16 from the bottom of the differential fluidized bed gasifier 16;

[0047] Step 3: In the differential fluidized bed gasifier 16, the high-temperature circulating material and the high-temperature superheated steam heat the differential fluidized bed gasifier 16 to 780 - 850 °C. The biomass char reacts with the high-temperature steam (the weight ratio of steam to biomass char = 1 - 3:1) at this temperature to generate syngas H2, CO, CO2, CH4, and trace H2S. The gas production rate of the biomass char is 2.5 - 3.0 Nm 3 / kg (where: the volume fraction of H2 is 75% - 77%, the volume fraction of CO is 7 - 8%, the volume fraction of CO2 is 6.5 - 8.5%, the volume fraction of CH4 is 6.5 - 8%, and the original H2S < 100 mg / Nm 3 ); At the same time, CaO and MgO formed after the calcination of limestone and dolomite react with H2S (the reaction time in the differential fluidized bed gasifier 16 is not less than 10 s), removing 90% of H2S, and H2S < 10 mg / Nm 3 (meeting the requirement that the subsequent water-gas shift reaction catalyst will not fail);

[0048] Step 4: The high-temperature syngas discharged from the top of the differential fluidized bed gasifier 16 enters the high-efficiency cyclone separator 14, where the circulating material carried in it is separated and returned to the differential fluidized bed gasifier 16. Then the syngas passes through the superheater 23 and the air preheater 24, and is cooled to 350 °C, and enters the dust collector 25 (the dust collector 25 can be an existing mature ceramic filter, metal mesh filter, or other dust collectors that can withstand temperatures above 350 °C. The dust removal efficiency of the dust collector 25 reaches more than 99.9%, and the dust content in the syngas ≤ 5 mg / m 3 ), and the dust-removed syngas (at a temperature of 350 °C) enters the high-temperature water vapor shift reactor 27 (WGS-1, reaction conditions: using the commercial catalyst SCST-221, 350 °C, SV = 1300 - 2700 h -1 ), the temperature rises to 380 - 450 °C and enters the air preheater 28, where the air is preheated to 250 - 300 °C. After the syngas temperature drops to 190 - 200 °C, it enters the low-temperature water vapor shift reactor 29 (WGS-2, reaction conditions: using the commercial catalyst SCST-231, 190 - 200 °C, SV = 4600 - 5100 h -1) With a steam / CO molar ratio ≥ 2, through high- and low-temperature water-gas shift reactions: CO + H2O = H2 + CO2, the total conversion rate of CO is over 95%; the syngas is heated to 250 - 260 °C, and then enters the air preheater - 30, where the air is preheated from room temperature to 130 - 150 °C, and the temperature of the syngas drops to 120 - 150 °C. Then the syngas enters the condenser 32 (existing mature technology), and the waste heat boiler 19 is used to feed water to condense the water vapor in the syngas (recovering the latent heat of vaporization in the steam to improve the thermal efficiency of the system); then the syngas enters the organic amine scrubber 33 (mature technology) to remove the remaining dust, trace H2S, and over 90% of CO2 in the syngas. The clean syngas temperature drops to 50 - 60 °C, and the organic amine aqueous solution regenerates after absorbing CO2 (heated to 120 - 150 °C, then CO2 and water vapor are desorbed, and after condensation, high-purity CO2 is separated to achieve CO2 capture); then the syngas enters the pressure swing adsorption system (PSA) 35 through the compressor 34 to obtain 99.9% H2, and the H2, CO, and CO2 contained in the exhaust gas of the pressure swing adsorption system 35 are sent to the circulating fluidized bed 12 for combustion to release heat.

[0049] The effect of the second specific embodiment is as follows: The present invention uses the 900 - 950 °C high-temperature circulating ash of the circulating fluidized bed 12 as the heat source, and the 550 - 600 °C superheated steam as the fluidization medium and reactant to convert biomass char into H2, realizing the high-value utilization of biomass char. At the same time, using the waste heat boiler 19 equipped with a back-pressure steam turbine generator set 20 for power generation has significant economic efficiency and innovation. In addition, a high-temperature water-gas shift reactor (WSG-1) 27, a low-temperature water-gas shift reactor (WSG-2) 29, an organic amine scrubber 33 for absorbing CO2, and a pressure swing adsorption system (PSA) 35 are used to obtain 99.9% hydrogen.

[0050] The third specific embodiment: As Figure 2 、 Figure 7 and Figure 8 shown, this embodiment discloses a biomass drum carbonization polygeneration coupled with steam gasification hydrogen production device, including a screw feeder 1, a drum carbonizer 2, a gas burner 3, a screw feeder 5, an air-tar cooler 7, a multi-stage indirect water-cooled wood vinegar cooler 8, a gas blower 9, a wood vinegar spray tower 10, a screw feeder 11-1, a screw feeder 11-2, a circulating fluidized bed 12, a high-efficiency cyclone separator 13, a high-efficiency cyclone separator 14, a differential fluidized bed gasifier 16, a waste heat boiler 19, a back-pressure steam turbine generator set 20, a superheater 23, an air preheater 24, a dust collector 25, a high-temperature water-gas shift reactor 27, an air preheater 28, a low-temperature water-gas shift reactor 29, an air preheater 30, a condenser 32, an organic amine scrubber 33, a compressor 34, and a pressure swing adsorption system (PSA) 35;

[0051] The first screw feeder 1 is a biomass screw feeder, the third screw feeder 11-1 is a biomass feeder, and the fourth screw feeder 11-2 is a circulating material feeder (the circulating material consists of limestone, dolomite and Ni catalyst, and the mass ratio of limestone, dolomite and Ni catalyst = 1:1:1); the discharge port of the first screw feeder 1 is communicated with the feed port at one end of the drum carbonizer 2, and the discharge port at the other end of the drum carbonizer 2 is communicated with the biomass carbon inlet 17 of the differential fluidized bed gasifier 16 through the second screw feeder 5; the pyrolysis gas outlet of the drum carbonizer 2 is communicated with the pyrolysis gas inlet of the air-tar cooler 7, the air outlet of the air-tar cooler 7 is communicated with the air inlet of the gas burner 3 through a pipeline, and the pyrolysis gas outlet of the air-tar cooler 7 is successively communicated with the multi-stage indirect water-cooled wood vinegar liquid cooler 8, the gas blower 9 and the pyrolysis gas inlet of the wood vinegar liquid spray tower 10. The pyrolysis gas outlet of the wood vinegar liquid spray tower 10 is communicated with the pyrolysis gas inlet of the gas burner 3 through a pipeline, and the outlet of the gas burner 3 is communicated with the furnace chamber 4 of the drum carbonizer 2 (the furnace chamber for the combustion of biomass pyrolysis gas);

[0052] The flue gas outlet at the top of the drum carbonizer 2 is communicated with the flue gas inlet of the circulating fluidized bed 12. The circulating fluidized bed 12 is an adiabatic combustion chamber. The discharge ports of the third screw feeder 11-1 and the fourth screw feeder 11-2 are communicated with the circulating fluidized bed 12. The flue gas outlet at the top of the circulating fluidized bed 12 is communicated with the flue gas inlet of the first high-efficiency cyclone separator 13. The discharge port at the lower end of the first high-efficiency cyclone separator 13 is respectively communicated with the first feed port of the differential fluidized bed gasifier 16 and the return port of the circulating fluidized bed 12 through the first return valve 15. The discharge port of the differential fluidized bed gasifier 16 is communicated with the return inlet of the circulating fluidized bed 12 through the second return valve 18;

[0053] The flue gas outlet at the top of the first high-efficiency cyclone separator 13 is communicated with the flue gas inlet of the waste heat boiler 19. The steam outlet of the waste heat boiler 19 is communicated with the steam inlet of the back-pressure steam turbine generator set 20. The exhaust port of the back-pressure steam turbine generator set 20 is communicated with the steam inlet of the superheater 23. The superheated steam outlet of the superheater 23 is communicated with the superheated steam inlet at the bottom of the differential fluidized bed gasifier 16;

[0054] The syngas outlet at the top of the differential fluidized bed gasifier 16 is connected to the syngas inlet of the high-efficiency cyclone separator II 14. The syngas outlet at the top of the high-efficiency cyclone separator II 14 is connected to the syngas inlet of the superheater 23. The syngas outlet of the superheater 23 is successively connected to the air preheater III 24, the dust collector 25, the high-temperature steam conversion reactor 27, the air preheater II 28, the low-temperature steam conversion reactor 29, the air preheater I 30, the condenser 32, the organic amine scrubber 33, the compressor 34, and the pressure swing adsorption system 35. The exhaust port of the pressure swing adsorption system 35 is connected to the inlet of the lower part of the circulating fluidized bed 12 through a pipeline. The discharge port at the lower part of the high-efficiency cyclone separator II 14 is connected to the second feed inlet at the lower part of the differential fluidized bed gasifier 16.

[0055] Furthermore, the feed water outlet of the waste heat boiler 19 is connected to the feed water inlet of the waste heat boiler 19 through the condenser 32. The feed water of the waste heat boiler 19 is preheated by the condenser 32 and then enters the waste heat boiler 19 through the feed water inlet of the waste heat boiler 19.

[0056] Specific Embodiment Four: As Figure 2 , Figure 7 and Figure 8 shown (operating temperature of the differential fluidized bed steam gasifier: 600 - 700 °C, in-situ CO2 absorption), this embodiment discloses a method for biomass drum carbonization polygeneration coupled with steam gasification to produce hydrogen. The method is implemented based on the device described in Specific Embodiment Three. The method includes the following steps:

[0057] Step One: The screw feeder I 1 feeds biomass (agricultural and forestry waste, feeding amount: 1 - 5 t / h) into the drum carbonizer 2 for dry distillation. The biomass carbon discharged from the drum carbonizer 2 is fed into the differential fluidized bed gasifier 16 (a biomass carbon inlet 17 is provided on the differential fluidized bed gasifier 16) through the screw feeder II 5 to produce hydrogen-rich syngas with steam as the gasifying agent. The pyrolysis gas generated by the drum carbonizer 2 first enters the air tar cooler 7 (to condense and recover tar as a chemical raw material). The air is preheated and then sent to the gas burner 3 to be mixed with the pyrolysis gas and sent into the furnace 4 of the drum carbonizer 2 for combustion and heat release (providing the heat required for the drum carbonization of the drum carbonizer 2). Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar cooler 8 (to condense and collect the wood vinegar, and after vacuum extraction technology, the wood vinegar is purified and used as a foliar fertilizer and pesticide) and the gas blower 9 to send the pyrolysis gas into the wood vinegar spray tower 10 (the purpose is to further reduce the tar content in the pyrolysis gas. The purified wood vinegar is used as the spray liquid, so that the tar content in the pyrolysis gas is less than 50 mg / Nm 3) Then it is sent into the gas burner 3 and sprayed into the furnace 4 of the drum carbonizer 2 for combustion (the combustion temperature in the furnace 4 of the drum carbonizer 2 reaches 1100 - 1200 °C). High-temperature flue gas at 800 - 850 °C is discharged from the flue gas outlet at the top of the drum carbonizer 2 and enters the furnace of the circulating fluidized bed 12. The screw feeder III 11-1 feeds the auxiliary fuel biomass into the circulating fluidized bed 12 for combustion. At the same time, the screw feeder IV 11-2 feeds the circulating material (the circulating material consists of limestone, dolomite, and Ni catalyst, and the mass ratio of limestone, dolomite, and Ni catalyst = 1:1:1) into the circulating fluidized bed 12 for calcination (the calcination product is used as bed material on the one hand and as a catalyst for the differential fluidized bed gasifier 16 on the other hand);

[0058] High-temperature air at 300 - 350 °C enters the circulating fluidized bed 12 from the air chamber at the bottom of the circulating fluidized bed 12 to assist combustion (the circulating fluidized bed 12 is an adiabatic combustion furnace, the fluidization velocity is 6 - 10 m / s, and the circulation ratio is 30 - 100). High-temperature flue gas at 900 - 950 °C coming out of the flue gas outlet at the top of the circulating fluidized bed 12 carries the circulating material (calcination products of limestone and dolomite and Ni catalyst) into the high-efficiency cyclone separator I 13. The circulating material is separated out. Part of it is sent back into the circulating fluidized bed 12 through the return valve I 15, and the other part is sent into the differential fluidized bed gasifier 16 through the return valve I 15;

[0059] Step 2: The high-temperature flue gas coming out of the flue gas outlet at the top of the high-efficiency cyclone separator I 13 enters the waste heat boiler 19. The steam generated by the waste heat boiler 19 is sent to the back-pressure steam turbine generator set 20 for power generation. The steam (with a pressure of 0.2 - 0.3 MPa and a temperature of 200 - 250 °C) discharged from the back-pressure steam turbine generator set 20 enters the superheater 23 and is heated to 400 - 450 °C, and then enters the differential fluidized bed gasifier 16 from the bottom of the differential fluidized bed gasifier 16;

[0060] Step 3: In the differential fluidized bed gasifier 16, the high-temperature circulating material and high-temperature superheated steam heat the differential fluidized bed gasifier 16 to 600 - 700 °C. The biomass charcoal discharged from the drum carbonizer 2 is sent into the differential fluidized bed gasifier 16 through the screw feeder II 5. The biomass charcoal reacts with the high-temperature steam under the action of the catalyst (calcination products of limestone, dolomite, and Ni catalyst) to generate syngas H2, CO, CO2, CH4, and H2S; CaO undergoes an in-situ absorption reaction with CO2 to generate CaCO3, promoting the forward progress of CO + H2O = H2 + CO2 (such that the volume fraction of H2 is 80 - 85%, the volume fraction of CO is 5 - 6%, the volume fraction of CO2 is 0 - 3%, the volume fraction of CH4 is 10%, and H2S < 100 mg / Nm 3 );The gas production rate of biomass charcoal is 2.0 - 2.5 m 3 / kg; At the same time, CaO reacts with H2S to form CaS (the reaction time in the differential fluidized bed gasifier 16 is not less than 10 s), removing 90% of H2S, so that the H2S in the syngas < 10 mg / Nm 3 (meeting the requirement that the subsequent water-gas shift catalyst does not deactivate); The circulating materials containing CaCO3, CaS and the unreacted biomass char (accounting for 10 - 15% of the total biomass char weight) enter the circulating fluidized bed 12 through the second return valve 18, so that CaCO3 decomposes into CaO and CO2, CaS decomposes into CaO and SO2, and after the Ni-based catalyst eliminates carbon deposition in the circulating fluidized bed 12, it enters the differential fluidized bed gasifier 16 together with CaO and MgO (the calcination products of limestone and dolomite) after being separated by the first high-efficiency cyclone separator 13;

[0061] Step 4: The syngas at 600 - 700 °C coming out from the top of the differential fluidized bed gasifier 16 first enters the second high-efficiency cyclone separator 14 to separate the circulating materials carried in it and return them to the differential fluidized bed gasifier 16. The syngas coming out from the top of the second high-efficiency cyclone separator 14 enters the superheater 23 and the third air preheater 24 and then cools down to 350 °C, and then enters the dust collector 25 (the dust collector 25 can be an existing mature ceramic filter or metal mesh filter or other dust collectors that can withstand temperatures above 350 °C. The dust collection efficiency of the dust collector 25 reaches more than 99.9%, and the dust content in the syngas ≤ 5 mg / m 3 ), and the dust-removed syngas (350 °C) enters the high-temperature water-gas shift reactor 27 (WGS-1, using the commercial catalyst SCST-221, 350 °C, SV = 1300 - 2700 h -1 ), the temperature rises to 380 - 450 °C and enters the second air preheater 28 to preheat the air to 250 - 300 °C. After the syngas temperature drops to 190 - 200 °C, it enters the low-temperature water-gas shift reactor 29 (WGS-2, using the commercial catalyst SCST-231, 190 - 200 °C, SV = 4600 - 5100 h -1),The steam / CO molar ratio ≥ 2. Through high- and low-temperature water-gas shift reactions: CO + H2O = H2 + CO2, the total conversion rate of CO is over 95%. The syngas is heated to 250 - 260 °C and then enters the air preheater - 30, where the air is preheated from room temperature to 130 - 150 °C, and the temperature of the syngas drops to 120 - 150 °C. Then the syngas enters the condenser 32 (existing mature technology), and the waste heat boiler 19 is used to feed water to condense the water vapor in the syngas (recovering the latent heat of vaporization in the steam to improve the system thermal efficiency). Then the syngas enters the organic amine scrubber 33 (mature technology) to remove the remaining dust, trace H2S, and over 90% of CO2 in the syngas. The temperature of the clean syngas drops to 50 - 60 °C. After the organic amine aqueous solution absorbs CO2, it is regenerated (heated to 120 - 150 °C, then CO2 and water vapor are desorbed, and after condensation, high-purity CO2 is separated to achieve CO2 capture). Then the syngas enters the pressure swing adsorption system 35 (PSA) through the compressor 34 to obtain 99.9% H2. The H2, CO, and CO2 contained in the exhaust gas of the pressure swing adsorption system 35 are sent to the circulating fluidized bed 2 for combustion to release heat.

[0062] Effect of the specific implementation method four: The biomass char generated by the biomass in the drum carbonizer 2 enters the differential fluidized bed gasifier 16, where it absorbs CO2 in situ at 600 - 700 °C, causing the reaction CO + H2O = CO2 + H2 to proceed in the forward direction. The CO2 concentration drops significantly to less than 3%, and the H2 concentration rises significantly to 80 - 85%, reducing the pressure on the subsequent high-temperature water-gas shift reactor 27, low-temperature water-gas shift reactor 29, and organic amine scrubber 33.

[0063] In the present invention, the flue gas outlet of the waste heat boiler 19 is connected to the chimney 22 through the induced draft fan 21; the dust removal port at the lower part of the dust collector 25 is connected to the ash bin 26; the air outlet of the blower - 6 is connected to the air inlet of the air tar condenser 7 through a pipeline; the air outlet of the blower - 31 is connected to the air inlet of the air preheater - 30 through a pipeline. The motor 36 drives the gear transmission mechanism 37 to rotate, and the rotating components of the drum carbonizer 2 are driven to rotate through the gear transmission mechanism 37.

[0064] The differential fluidized bed structure in the present invention has been disclosed in the invention patent with the publication number CN102876339B, publication date December 25, 2013, and title "An apparatus for gasification and cracking reactions".

[0065] The above is only the preferred specific implementation method of the present invention patent, but the protection scope of the present invention patent is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention patent, according to the technical solution and inventive concept of the present invention patent, making equivalent substitutions or changes, should be covered within the protection scope of the present invention patent.

Claims

1. A biomass rotary carbonization polygeneration coupled with steam gasification hydrogen production device, characterized in that: It includes screw feeder 1 (1), drum carbonizer (2), gas burner (3), screw feeder 2 (5), air-tar cooler (7), multi-stage indirect water-cooled wood vinegar liquid cooler (8), gas blower (9), wood vinegar liquid spray tower (10), screw feeder 3 (11-1), screw feeder 4 (11-2), circulating fluidized bed (12), high-efficiency cyclone separator 1 (13), high-efficiency cyclone separator 2 (14), differential fluidized bed gasifier (16), waste heat boiler (19), back-pressure steam turbine generator set (20), superheater (23), air preheater 3 (24), dust collector (25), high-temperature water vapor shift reactor (27), air preheater 2 (28), low-temperature water vapor shift reactor (29), air preheater 1 (30), condenser (32), organic amine scrubber (33), compressor (34) and pressure swing adsorption system (35); The first screw feeder (1) is a biomass screw feeder, the third screw feeder (11-1) is an auxiliary fuel feeder, and the fourth screw feeder (11-2) is a circulating material feeder. The circulating material consists of limestone and dolomite. The discharge port of the first screw feeder (1) is communicated with the feed port at one end of the drum carbonizer (2), and the discharge port at the other end of the drum carbonizer (2) is communicated with the biomass carbon inlet (17) of the differential fluidized bed gasifier (16) through the second screw feeder (5). The pyrolysis gas outlet of the drum carbonizer (2) is communicated with the pyrolysis gas inlet of the air-tar cooler (7). The air outlet of the air-tar cooler (7) is communicated with the air inlet of the gas burner (3) through a pipeline. The pyrolysis gas outlet of the air-tar cooler (7) is successively communicated with the multi-stage indirect water-cooled wood vinegar liquid cooler (8), the gas blower (9), and the pyrolysis gas inlet of the wood vinegar liquid spray tower (10). The pyrolysis gas outlet of the wood vinegar liquid spray tower (10) is communicated with the pyrolysis gas inlet of the gas burner (3) through a pipeline, and the outlet of the gas burner (3) is communicated with the furnace chamber (4) of the drum carbonizer (2). The flue gas outlet at the top of the drum carbonizer (2) is communicated with the flue gas inlet of the circulating fluidized bed (12). The circulating fluidized bed (12) is an adiabatic combustion chamber. The discharge ports of the third screw feeder (11-1) and the fourth screw feeder (11-2) are communicated with the circulating fluidized bed (12). The flue gas outlet at the top of the circulating fluidized bed (12) is communicated with the flue gas inlet of the first high-efficiency cyclone separator (13). The discharge port at the lower end of the first high-efficiency cyclone separator (13) is communicated with the first feed port of the differential fluidized bed gasifier (16) through the first return valve (15). The discharge port of the differential fluidized bed gasifier (16) is communicated with the return feed inlet of the circulating fluidized bed (12) through the second return valve (18). The flue gas outlet at the top of the first high-efficiency cyclone separator (13) is communicated with the flue gas inlet of the waste heat boiler (19). The steam outlet of the waste heat boiler (19) is communicated with the steam inlet of the back-pressure steam turbine generator set (20). The exhaust port of the back-pressure steam turbine generator set (20) is communicated with the steam inlet of the superheater (23). The superheated steam outlet of the superheater (23) is communicated with the superheated steam inlet at the bottom of the differential fluidized bed gasifier (16). The syngas outlet at the top of the differential fluidized bed gasifier (16) is communicated with the syngas inlet of the second high-efficiency cyclone separator (14). The syngas outlet at the top of the second high-efficiency cyclone separator (14) is communicated with the syngas inlet of the superheater (23). The syngas outlet of the superheater (23) is successively communicated with the third air preheater (24), the dust collector (25), the high-temperature steam-water shift reactor (27), the second air preheater (28), the low-temperature steam-water shift reactor (29), the first air preheater (30), the condenser (32), the organic amine scrubber (33), the compressor (34), and the pressure swing adsorption system (35). The exhaust port of the pressure swing adsorption system (35) is communicated with the air inlet at the lower part of the circulating fluidized bed (12) through a pipeline.The discharge port at the lower part of the high-efficiency cyclone separator II (14) is connected to the second feed port at the lower part of the differential fluidized bed gasifier (16).; 2. The biomass drum carbonization poly-generation coupled with steam gasification hydrogen production device according to claim 1, wherein: The feed water outlet of the waste heat boiler (19) is connected to the feed water inlet of the waste heat boiler (19) through the condenser (32).

3. A method for co-production coupling steam gasification to produce hydrogen from biomass drum carbonization, characterized in that, The method is implemented based on the device described in claim 2, and the method includes the following steps: Step 1: Screw feeder 1 (1) feeds biomass into the drum carbonizer (2) for dry distillation. The biomass charcoal discharged from the drum carbonizer (2) is fed into the differential fluidized bed gasifier (16) through screw feeder 2 (5). There is at least 1 drum carbonizer (2). Hydrogen-rich syngas is generated with water vapor as the gasifying agent. The pyrolysis gas generated by the drum carbonizer (2) first enters the air-tar cooler (7). After the air is preheated, it is sent to the gas burner (3) to be mixed with the pyrolysis gas and then sent into the furnace (4) of the drum carbonizer (2) for combustion and heat release. Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar liquid cooler (8) and the gas blower (9) to send the pyrolysis gas into the wood vinegar liquid spray tower (10), and then sent to the gas burner (3) and sprayed into the furnace (4) of the drum carbonizer (2) for combustion. High-temperature flue gas at 800-850 °C is discharged from the top flue gas outlet of the drum carbonizer (2) and enters the furnace (4) of the circulating fluidized bed (12). Screw feeder 3 (11-1) feeds biomass into the circulating fluidized bed (12) for combustion, and at the same time, screw feeder 4 (11-2) feeds the circulating material into the circulating fluidized bed (12) for calcination; High-temperature air at 400-450 °C enters the circulating fluidized bed (12) from the bottom air chamber of the circulating fluidized bed (12) to assist combustion. High-temperature flue gas at 900-950 °C carrying the circulating material comes out from the flue gas outlet at the top of the circulating fluidized bed (12) and enters the high-efficiency cyclone separator 1 (13) to separate the circulating material, and then is sent into the differential fluidized bed gasifier (16) through the return valve 1 (15). At the same time, the biomass charcoal discharged from the drum carbonizer (2) is fed into the differential fluidized bed gasifier (16) through screw feeder 2 (5) and reacts with the high-temperature water vapor at 550-600 °C fed in to generate syngas at a bed temperature of 780-850 °C; Step 2: The high-temperature flue gas discharged from the flue gas outlet at the top of the high-efficiency cyclone separator I (13) enters the waste heat boiler (19). The steam generated by the waste heat boiler (19) is sent to the back-pressure steam turbine generator set (20) for power generation. The steam discharged from the back-pressure steam turbine generator set (20) enters the superheater (23), is heated to 550 - 600 °C, and then enters the differential fluidized bed gasifier (16) from the bottom of the differential fluidized bed gasifier (16). Step 3: In the differential fluidized bed gasifier (16), the high-temperature circulating material and high-temperature superheated steam heat the differential fluidized bed gasifier (16) to 780 - 850 °C, and the mass ratio of steam to biomass char = 1 - 3:1; the biomass char reacts with the high-temperature steam at this temperature to generate syngas H2, CO, CO2, CH4 and trace amounts of H2S, and the gas production rate of biomass char is 2.5 - 3.0 Nm 3 / kg; at the same time, CaO and MgO formed after the calcination of limestone and dolomite react with H2S to remove 90% of H2S, and H2S < 10 mg / Nm 3 ; Step 4: The high-temperature synthesis gas discharged from the top of the differential fluidized bed gasifier (16) enters the high-efficiency cyclone separator II (14). The circulating materials carried therein are separated and returned to the differential fluidized bed gasifier (16). Then, the synthesis gas passes through the superheater (23) and the air preheater III (24), and is cooled to 350 °C. Then it enters the dust collector (25). After dust removal, the synthesis gas enters the high-temperature steam-water shift reactor (27), is heated to 380 - 450 °C, and enters the air preheater II (28), where the air is preheated to 250 - 300 °C. The synthesis gas is cooled to 190 - 200 °C and then enters the low-temperature steam-water shift reactor (29). The steam / CO molar ratio ≥ 2. The total conversion rate of CO in the high-temperature and low-temperature steam-water shift reactions: CO + H2O = H2 + CO2 is over 95%. The synthesis gas is heated to 250 - 260 °C, and then enters the air preheater I (30), where the air is preheated from room temperature to 130 - 150 °C. The synthesis gas is cooled to 120 - 150 °C. Then the synthesis gas enters the condenser (32), and the steam in the synthesis gas is condensed by using the feed water of the waste heat boiler (19). Then the synthesis gas enters the organic amine scrubber (33) to remove the remaining dust, trace H2S and over 90% of CO2 in the synthesis gas. The clean synthesis gas is cooled to 50 - 60 °C, and the organic amine aqueous solution is regenerated after absorbing CO2. Then the synthesis gas enters the pressure swing adsorption system (35) through the compressor (34) to obtain 99.9% H2. The exhaust gas of the pressure swing adsorption system (35) is sent to the circulating fluidized bed (12) for combustion to release heat.

4. A biomass drum carbonization poly-generation coupled steam gasification hydrogen production device, characterized in that: It includes screw feeder I (1), drum carbonizer (2), gas burner (3), screw feeder II (5), air-tar cooler (7), multi-stage indirect water-cooled wood vinegar cooler (8), gas blower (9), wood vinegar spray tower (10), screw feeder III (11-1), screw feeder IV (11-2), circulating fluidized bed (12), high-efficiency cyclone separator I (13), high-efficiency cyclone separator II (14), differential fluidized bed gasifier (16), waste heat boiler (19), back-pressure steam turbine generator set (20), superheater (23), air preheater III (24), dust collector (25), high-temperature steam-water shift reactor (27), air preheater II (28), low-temperature steam-water shift reactor (29), air preheater I (30), condenser (32), organic amine scrubber (33), compressor (34) and pressure swing adsorption system (35); The first screw feeder (1) is a biomass screw feeder, the third screw feeder (11-1) is a biomass feeder, and the fourth screw feeder (11-2) is a recycled material feeder; the discharge port of the first screw feeder (1) is connected to the feed port at one end of the drum carbonizer (2), and the discharge port at the other end of the drum carbonizer (2) is connected to the biomass carbon inlet (17) of the differential fluidized bed gasifier (16) through the second screw feeder (5); the pyrolysis gas outlet of the drum carbonizer (2) is connected to the pyrolysis gas inlet of the air-tar cooler (7), the air outlet of the air-tar cooler (7) is connected to the air inlet of the gas burner (3) through a pipeline, the pyrolysis gas outlet of the air-tar cooler (7) is successively connected to the multi-stage indirect water-cooled wood vinegar cooler (8), the gas blower (9), and the pyrolysis gas inlet of the wood vinegar spray tower (10), the pyrolysis gas outlet of the wood vinegar spray tower (10) is connected to the pyrolysis gas inlet of the gas burner (3) through a pipeline, and the outlet of the gas burner (3) is connected to the furnace (4) of the drum carbonizer (2); the flue gas outlet at the top of the drum carbonizer (2) is connected to the flue gas inlet of the circulating fluidized bed (12), the circulating fluidized bed (12) is an adiabatic combustion chamber, the discharge ports of the third screw feeder (11-1) and the fourth screw feeder (11-2) are connected to the circulating fluidized bed (12), the flue gas outlet at the top of the circulating fluidized bed (12) is connected to the flue gas inlet of the first high-efficiency cyclone separator (13), the discharge port at the lower end of the first high-efficiency cyclone separator (13) is respectively connected to the first feed port of the differential fluidized bed gasifier (16) and the return port of the circulating fluidized bed (12) through the first return valve (15), and the discharge port of the differential fluidized bed gasifier (16) is connected to the return inlet of the circulating fluidized bed (12) through the second return valve (18); the flue gas outlet at the top of the first high-efficiency cyclone separator (13) is connected to the flue gas inlet of the waste heat boiler (19), the steam outlet of the waste heat boiler (19) is connected to the steam inlet of the back-pressure steam turbine generator set (20), the exhaust port of the back-pressure steam turbine generator set (20) is connected to the steam inlet of the superheater (23), and the superheated steam outlet of the superheater (23) is connected to the superheated steam inlet at the bottom of the differential fluidized bed gasifier (16); the syngas outlet at the top of the differential fluidized bed gasifier (16) is connected to the syngas inlet of the second high-efficiency cyclone separator (14), the syngas outlet at the top of the second high-efficiency cyclone separator (14) is connected to the syngas inlet of the superheater (23), and the syngas outlet of the superheater (23) is successively connected to the third air preheater (24), the dust collector (25), the high-temperature steam reforming reactor (27), the second air preheater (28), the low-temperature steam reforming reactor (29), the first air preheater (30), the condenser (32), the organic amine scrubber (33), the compressor (34), and the pressure swing adsorption system (35), and the exhaust port of the pressure swing adsorption system (35) is connected to the inlet at the lower part of the circulating fluidized bed (12) through a pipeline;The discharge port at the lower part of the high-efficiency cyclone separator II (14) is communicated with the second feed port at the lower part of the differential fluidized bed gasifier (16).; 5. The biomass drum carbonization poly-generation coupled with steam gasification hydrogen production device according to claim 4, characterized in that: The feed water outlet of the waste heat boiler (19) is connected to the feed water inlet of the waste heat boiler (19) through the condenser (32).

6. A method for biomass drum carbonization multi-generation coupled with steam gasification to produce hydrogen, characterized in that, The method is implemented based on the device described in claim 5, and the method includes the following steps: Step 1: The screw feeder 1 (1) feeds biomass into the drum carbonizer (2) for dry distillation. The biomass charcoal discharged from the drum carbonizer (2) is fed into the differential fluidized bed gasifier (16) through the screw feeder 2 (5) to produce hydrogen-rich syngas with steam as the gasifying agent. The pyrolysis gas generated by the drum carbonizer (2) first enters the air-tar cooler (7). After the air is preheated, it is sent to the gas burner (3) to be mixed with the pyrolysis gas and then sent into the furnace (4) of the drum carbonizer (2) for combustion and heat release. Then, the pyrolysis gas successively passes through the multi-stage indirect water-cooled wood vinegar liquid cooler (8) and the gas blower (9) to send the pyrolysis gas into the wood vinegar liquid spray tower (10), and then into the gas burner (3) and sprayed into the furnace (4) of the drum carbonizer (2) for combustion. The high-temperature flue gas at 800 - 850 °C discharged from the flue gas outlet at the top of the drum carbonizer (2) enters the furnace (4) of the circulating fluidized bed (12). The screw feeder 3 (11-1) feeds the auxiliary fuel biomass into the circulating fluidized bed (12) for combustion. At the same time, the screw feeder 4 (11-2) feeds the circulating material into the circulating fluidized bed (12) for calcination; The high-temperature air at 300 - 350 °C enters the circulating fluidized bed (12) from the bottom air chamber of the circulating fluidized bed (12) for combustion support. The high-temperature flue gas at 900 - 950 °C carrying the circulating material comes out from the flue gas outlet at the top of the circulating fluidized bed (12) and enters the high-efficiency cyclone separator 1 (13) to separate the circulating material. Part of it is sent back into the circulating fluidized bed (12) through the return valve 1 (15), and the other part is sent into the differential fluidized bed gasifier (16) through the return valve 1 (15); Step 2: The high-temperature flue gas coming out from the flue gas outlet at the top of the high-efficiency cyclone separator 1 (13) enters the waste heat boiler (19). The steam generated by the waste heat boiler (19) is sent to the back-pressure steam turbine generator set (20) for power generation. The steam discharged from the back-pressure steam turbine generator set (20) enters the superheater (23) and is heated to 400 - 450 °C, and then enters the differential fluidized bed gasifier (16) from the bottom of the differential fluidized bed gasifier (16); Step 3: In the differential fluidized bed gasifier (16), the high-temperature circulating material and high-temperature superheated steam heat the differential fluidized bed gasifier (16) to 600 - 700 °C. The biomass char discharged from the drum carbonizer (2) is fed into the differential fluidized bed gasifier (16) through the second screw feeder (5). The mass ratio of steam to biomass char = 1 - 3:

1. The biomass char and high-temperature steam react under the action of a catalyst to generate syngas H2, CO, CO2, CH4, and H2S. CaO undergoes an in-situ absorption reaction with CO2 to form CaCO3, promoting the forward reaction of CO + H2O = H2 + CO2. The gas production rate of biomass char is 2.0 - 2.5 Nm 3 / kg. At the same time, CaO reacts with H2S to form CaS, removing 90% of H2S, so that H2S in the syngas < 10 mg / Nm 3 ; The circulating material containing CaCO3, CaS, and the unreacted biomass char enter the circulating fluidized bed (12) through the second return valve (18), causing CaCO3 to decompose into CaO and CO2, and CaS to decompose into CaO and SO2. After the Ni-based catalyst removes carbon deposition in the circulating fluidized bed (12), it is separated from CaO and MgO through the first high-efficiency cyclone separator (13) and then enters the differential fluidized bed gasifier (16); Step 4: The syngas at 600 - 700 °C coming out from the top of the differential fluidized bed gasifier (16) first enters the high-efficiency cyclone separator II (14), where the circulating materials carried in it are separated and returned to the differential fluidized bed gasifier (16). The syngas coming out from the top of the high-efficiency cyclone separator II (14) enters the superheater (23) and the air preheater III (24), and then the temperature drops to 350 °C. Then it enters the dust collector (25). After dust removal, the syngas enters the high-temperature steam reforming reactor (27), and the temperature rises to 380 - 450 °C and enters the air preheater II (28), where the air is preheated to 250 - 300 °C. After the temperature of the syngas drops to 190 - 200 °C, it enters the low-temperature steam reforming reactor (29), with a steam / CO molar ratio ≥ 2. After the high- and low-temperature steam reforming reactions: CO + H2O = H2 + CO2, the total conversion rate of CO is over 95%. The temperature of the syngas rises to 250 - 260 °C, and then enters the air preheater I (30), where the air is preheated from room temperature to 130 - 150 °C. After the temperature of the syngas drops to 120 - 150 °C, the syngas then enters the condenser (32), and the steam in the syngas is condensed using the feed water of the waste heat boiler (19). Then the syngas enters the organic amine scrubber (33) to remove the remaining dust, trace H2S and over 90% of CO2 in the syngas. The temperature of the clean syngas drops to 50 - 60 °C, and the organic amine aqueous solution is regenerated after absorbing CO2. Then the syngas enters the pressure swing adsorption system (35) through the compressor (34) to obtain 99.9% H2, and the exhaust gas of the pressure swing adsorption system (35) is sent to the circulating fluidized bed for combustion to release heat.

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