Biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification hydrogen production device and method

Abstract

Biomass reciprocating grate exhaust gasification power generation coupled with steam gasification hydrogen production device and method, belonging to the fields of chemical engineering and power generation. The hopper is arranged in front of the reciprocating grate, the primary air preheater is communicated with the lower air chamber of the reciprocating grate, the reciprocating grate gasifier is communicated with the secondary air preheater, and the outlet of the secondary combustion chamber is communicated with the superheater 1, the economizer, and the primary and secondary air preheaters; the end of the reciprocating grate is communicated with the differential fluidized bed gasifier through the first screw feeder, the second screw feeder is communicated with the circulating fluidized bed, the circulating fluidized bed is communicated with the differential fluidized bed gasifier through the first high-efficiency cyclone separator, and the differential fluidized bed gasifier is communicated with the circulating fluidized bed; the differential fluidized bed gasifier is communicated with the second high-efficiency cyclone separator, and the second high-efficiency cyclone separator is communicated with the superheater 2, the air preheater 3, the dust collector, the high-temperature WGS-1, the air preheater 2, the low-temperature WGS-2, the air preheater 1, the condenser, the organic amine scrubber, the compressor, and the pressure swing adsorption system. The present invention is used for gasification hydrogen production.

Description

Technical Field

[0001] The invention belongs to the technical fields of chemical engineering and power generation, and particularly relates to a biomass reciprocating grate exhaust gasification power generation and steam gasification hydrogen production coupling device and method. Background Art

[0002] There is a problem in directly gasifying biomass to produce hydrogen that it is difficult to remove tar from the syngas. Tar not only causes fouling and blockage of heat exchange equipment, but also causes catalyst carbon deposition. Removing tar from the syngas requires a high cost. For this reason, the invention proposes a biomass reciprocating grate exhaust gasification power generation and steam gasification hydrogen production coupling process to solve the problem of high-value utilization of biomass. Summary of the Invention

[0003] The purpose of the invention is to propose a biomass reciprocating grate exhaust gasification power generation and steam gasification hydrogen production coupling device and method. The invention uses the high-temperature circulating ash of a circulating fluidized bed as a heat source and high-temperature steam as a gasification medium to gasify the biomass char generated by the reciprocating grate exhaust gasifier in a differential fluidized bed to produce hydrogen, realizing the high-value utilization of biomass.

[0004] The invention proposes that the biomass reciprocating grate exhaust gasifies to produce biomass char, avoiding the tar problem in gasifying the biomass char with steam. At the same time, the gas generated by gasification is burned in a secondary combustion chamber to generate high-temperature and high-pressure steam, which is used to drive a steam turbine generator set to generate electricity.

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

[0006] Solution 1: A biomass reciprocating grate exhaust gasification power generation and steam gasification hydrogen production coupling device, comprising a hopper, a reciprocating grate exhaust gasifier, a screw feeder 1, a economizer, a superheater 1, a primary air preheater, a secondary air preheater, a screw feeder 2, a screw feeder 3, a circulating fluidized bed, a high-efficiency cyclone separator 1, a high-efficiency cyclone separator 2, a differential fluidized bed gasifier, a waste heat boiler, a steam turbine generator set, a superheater 2, an air preheater 3, a dust collector, a high-temperature steam shift reactor, an air preheater 2, a low-temperature steam shift reactor, an air preheater 1, a condenser, an organic amine scrubber, a compressor and a pressure swing adsorption system;

[0007] The reciprocating grate gasifier is provided with a reciprocating grate at the bottom, a secondary air inlet on the side wall of the reciprocating grate gasifier. The space from above the reciprocating grate to below the secondary air inlet is the gasification chamber, and the space above the secondary air inlet is the secondary combustion chamber; the hopper is a biomass hopper, and the discharge port of the hopper is arranged at the front end inlet of the reciprocating grate. The primary air preheater is connected to the lower air chamber of the reciprocating grate through a pipeline, the secondary air inlet is connected to the secondary air preheater through a pipeline, and the flue gas outlet at the top of the secondary combustion chamber is successively connected to the first superheater, the economizer, the primary air preheater and the secondary air preheater. The first superheater, the economizer, the primary air preheater and the secondary air preheater are all installed in the tail flue of the reciprocating grate gasifier; the end of the reciprocating grate is connected to the biomass carbon feed port of the differential fluidized bed gasifier through a screw feeder 1. The screw feeder 2 is an auxiliary fuel feeder, and the screw feeder 3 is a circulating material feeder. The circulating material consists of limestone and dolomite. The discharge ports of the screw feeder 2 and the screw feeder 3 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 high-efficiency cyclone separator 1. The discharge port at the lower end of the high-efficiency cyclone separator 1 is connected to the first feed port of the differential fluidized bed gasifier through a return valve 1. The discharge port of the differential fluidized bed gasifier is connected to the return inlet of the circulating fluidized bed through a return valve 2; the flue gas outlet at the top of the high-efficiency cyclone separator 1 is connected to the flue gas inlet of the waste heat boiler. The steam outlet of the waste heat boiler and the high-temperature and high-pressure steam outlet of the reciprocating grate gasifier are connected to the steam inlet of the steam turbine generator set through a main pipe. The low-pressure cylinder extraction port of the steam turbine generator set is connected to the steam inlet of the second superheater through a pipeline. The superheated steam outlet of the second 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 high-efficiency cyclone separator 2. The syngas outlet at the top of the high-efficiency cyclone separator 2 is connected to the syngas inlet of the second superheater. The syngas outlet of the second superheater is successively 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 high-efficiency cyclone separator 2 is connected to the second feed port at the lower part of the differential fluidized bed gasifier.

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

[0009] A method for biomass reciprocating grate gasification power generation coupled with steam gasification for hydrogen production, the method comprising the following steps:

[0010] Step 1: Biomass in the hopper enters the gasification chamber through the reciprocating grate for gasification. The primary air is preheated and then enters the air chamber at the lower part of the reciprocating grate. The gas generated in the gasification chamber is mixed with the secondary air and then burns and releases heat in the secondary combustion chamber. The high-temperature flue gas coming out of the secondary combustion chamber successively enters the first superheater, economizer, primary air preheater and secondary air preheater, and then goes to the tail treatment system. The biomass charcoal discharged from the end of the reciprocating grate is sent into the differential fluidized bed gasifier through the first screw feeder. High-temperature steam reacts with the biomass charcoal to produce hydrogen-rich syngas. The second screw feeder sends the biomass into the circulating fluidized bed for combustion. At the same time, the third screw feeder sends the circulating material into the circulating fluidized bed for calcination.

[0011] 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 coming out of the flue gas outlet at the top of the circulating fluidized bed carries the circulating material into the first high-efficiency cyclone separator to separate the circulating material, and then sends it into the differential fluidized bed gasifier through the first return valve. The biomass charcoal sent into the differential fluidized bed gasifier through the first screw feeder reacts with the high-temperature steam at 550 - 600 °C, and syngas is generated at a bed temperature of 780 - 850 °C.

[0012] Step 2: The high-temperature flue gas coming out of 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 converges with the high-temperature and high-pressure steam generated by the gasification and combustion of the biomass reciprocating grate, and is sent to the steam turbine generator set for power generation. The extraction steam from the low-pressure cylinder of the steam turbine generator set enters the second superheater and is heated to 550 - 600 °C, and then enters the differential fluidized bed gasifier from the bottom air chamber of the differential fluidized bed gasifier.

[0013] Step 3: In the differential fluidized bed gasifier, the high-temperature circulating material and 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 in it are separated and returned to the differential fluidized bed gasifier. Then the syngas passes through the superheater II and the air preheater III and is cooled to 300 - 350 °C, and then enters the dust collector. After dust removal, the syngas enters the high-temperature steam reforming reactor, and after the temperature rises to 380 - 450 °C, it enters the air preheater II to preheat the air to 250 - 300 °C. After the syngas temperature drops to 190 - 200 °C, it enters the low-temperature steam reforming reactor, with the steam / CO molar ratio ≥ 2. For the high-temperature 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 air preheater I to preheat the air from room temperature to 130 - 150 °C. After the syngas temperature drops to 120 - 150 °C, the syngas then enters the condenser, where the steam in the syngas is condensed by the feed water of the waste heat boiler and 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 the 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 reciprocating grate gasification power generation coupled with steam gasification hydrogen production device, including a hopper, a reciprocating grate gasifier, a screw feeder I, a economizer, a superheater I, a primary air preheater, a secondary air preheater, a screw feeder II, a screw feeder III, 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 steam turbine generator set, a superheater II, an air preheater III, a dust collector, a high-temperature steam reforming reactor, an air preheater II, a low-temperature steam reforming reactor, an air preheater I, a condenser, an organic amine scrubber, a compressor and a pressure swing adsorption system;

[0016] The reciprocating grate gasifier is provided with a reciprocating grate at the bottom, a secondary air inlet on the side wall of the reciprocating grate gasifier, a gasification chamber in the space from above the reciprocating grate to below the secondary air inlet, and a secondary combustion chamber in the space above the secondary air inlet. The hopper is a biomass hopper, and the discharge port of the hopper is arranged at the front end inlet of the reciprocating grate. The primary air preheater is connected to the lower air chamber of the reciprocating grate through a pipeline, the secondary air inlet is connected to the secondary air preheater through a pipeline, and the flue gas outlet at the top of the secondary combustion chamber is successively connected to the first superheater, the economizer, the primary air preheater, and the secondary air preheater. The first superheater, the economizer, the primary air preheater, and the secondary air preheater are all installed in the tail flue of the reciprocating grate gasifier; the end of the reciprocating grate is connected to the biomass charcoal feed port of the differential fluidized bed gasifier through a screw feeder 1. The screw feeder 2 is an auxiliary fuel feeder, and the screw feeder 3 is a circulating material feeder. The circulating material consists of limestone, dolomite, and Ni-based catalyst. The discharge ports of the screw feeder 2 and the screw feeder 3 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 high-efficiency cyclone separator 1. The discharge port at the lower end of the high-efficiency cyclone separator 1 is respectively connected to the first feed port of the differential fluidized bed gasifier and the return port of the circulating fluidized bed through a return valve 1. The discharge port of the differential fluidized bed gasifier is connected to the return inlet of the circulating fluidized bed through a return valve 2; the flue gas outlet at the top of the high-efficiency cyclone separator 1 is connected to the flue gas inlet of the waste heat boiler. The steam outlet of the waste heat boiler and the high-temperature and high-pressure steam outlet of the reciprocating grate gasifier are connected to the steam inlet of the steam turbine generator set through a main pipe. The low-pressure cylinder extraction port of the steam turbine generator set is connected to the steam inlet of the second superheater through a pipeline, and the superheated steam outlet of the second superheater is connected to the superheated steam inlet of the bottom air chamber 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 high-efficiency cyclone separator 2. The syngas outlet at the top of the high-efficiency cyclone separator 2 is connected to the syngas inlet of the second superheater. The syngas outlet of the second superheater is successively connected to 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. 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 high-efficiency cyclone separator 2 is connected to the second feed port at the lower part of the differential fluidized bed gasifier.

[0017] Furthermore, the feed water outlet of the waste heat boiler is connected to the feed water inlet of the waste heat boiler through a condenser.

[0018] The method for coupling biomass reciprocating grate gasification power generation with steam gasification for hydrogen production includes the following steps:

[0019] Step 1: Biomass in the hopper enters the gasification chamber through the reciprocating grate for gasification. The primary air is preheated and then enters the air chamber at the lower part of the reciprocating grate. The gas generated in the gasification chamber is mixed with the secondary air and then burns and releases heat in the secondary combustion chamber. The high-temperature flue gas coming out of the secondary combustion chamber successively enters the first superheater, economizer, primary air preheater and secondary air preheater, and then goes to the tail treatment system. The biomass char discharged from the end of the reciprocating grate is sent into the differential fluidized bed gasifier through the first screw feeder. High-temperature steam reacts with the biomass char to produce hydrogen-rich syngas. The second screw feeder sends the biomass into the circulating fluidized bed for combustion. The amount of biomass is adjusted to ensure that the outlet temperature of the circulating fluidized bed is 900 - 950 °C, and the feeding amount is determined by the load. At the same time, the third screw feeder sends the circulating material into the circulating fluidized bed for calcination.

[0020] High-temperature air at 300 - 350 °C enters the circulating fluidized bed from the bottom air chamber of the circulating fluidized bed to support 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. Part of it is sent back into the circulating fluidized bed through the first return valve, and the other part is sent into the differential fluidized bed gasifier through the first return valve.

[0021] Step 2: The high-temperature flue gas coming out of 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 combined with the high-temperature and high-pressure steam generated by the gasification and combustion of the biomass reciprocating grate and sent together to the steam turbine generator set for power generation. The extraction steam from the low-pressure cylinder of the steam turbine generator set enters the second superheater and is heated to 400 - 450 °C, and then the superheated steam enters the differential fluidized bed gasifier from the bottom air chamber of the differential fluidized bed gasifier.

[0022] Step 3: In the differential fluidized bed gasifier, the high-temperature circulating material and high-temperature superheated steam heat the differential fluidized bed gasifier to 600 - 700 °C. The biomass char discharged from the reciprocating grate is sent into the differential fluidized bed gasifier through the first screw feeder. The biomass char reacts with the high-temperature steam under the action of a catalyst to produce syngas H2, CO, CO2, CH4 and H2S. CaO reacts with CO2 in-situ to form CaCO3, promoting the forward reaction of CO + H2O = H2 + CO2. The mass ratio of steam to biomass char = 1 - 3:1, and 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 enters the circulating fluidized bed through the second return valve, causing CaCO3 to decompose into CaO and CO2, and CaS to decompose into CaO and SO2. The Ni-based catalyst removes carbon deposition in the circulating fluidized bed and then 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 high - efficiency cyclone separator II, where the circulating materials carried in it are separated and returned to the differential fluidized bed gasifier. The syngas coming out from the top of the high - efficiency cyclone separator II enters the superheater II and the air preheater III, and then the temperature drops to 300 - 350 °C and enters the dust collector. After dust removal, the syngas enters the high - temperature steam shift reactor, 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 enters the low - temperature steam shift reactor, with a steam / CO molar ratio ≥ 2. Through the 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 I, where the air is preheated from room temperature to 130 - 150 °C. The temperature of the syngas drops to 120 - 150 °C. Then the syngas enters the condenser and the organic amine scrubber 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 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 avoids the tar problem in biomass gasification for hydrogen production, uses a reciprocating furnace exhaust gasifier to produce biomass char, gasifies the biomass char with steam to produce H2, and at the same time burns the gas in the secondary combustion chamber to generate high - temperature and high - pressure steam for power generation, realizing the high - value utilization of biomass. The present invention uses the heat of high - temperature circulating ash at 900 - 950 °C, plus superheated steam at 550 - 600 °C as the fluidization medium and reactant to gasify biomass char in the differential fluidized bed gasifier to produce H2, greatly reducing the equipment investment cost, and having significant innovation and economy. 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 reaches over 85%. After absorbing CO2 by organic amine, the volume fraction of H2 in the syngas reaches over 90%. Description of the Drawings

[0025] Figure 1 is the structural schematic of the biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification for hydrogen production device of the present invention Figure 1 The operating temperature of the differential fluidized bed gasifier: 780 - 850 °C;

[0026] Figure 2 is the structural schematic of the biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification for hydrogen production device of the present invention Figure 2, Operating temperature of the differential fluidized bed gasifier: 600 - 700 °C, in-situ CO2 absorption;

[0027] Figure 3 Yes Figure 1 Partial enlarged view of area A of

[0028] Figure 4 Yes Figure 1 Partial enlarged view of area B of

[0029] Figure 5 Yes Figure 1 Partial enlarged view of area C of

[0030] Figure 6 Yes Figure 2 Partial enlarged view of area D of

[0031] Figure 7 Yes Figure 2 Partial enlarged view of area E of

[0032] Figure 8 Yes Figure 2 Partial enlarged view of area F of

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

[0034] Hopper 1, reciprocating grate 2, gasification chamber 3, secondary air inlet 4, secondary combustion chamber 5, screw feeder 1 6, economizer 7, superheater 1 8, primary air preheater 9, secondary air preheater 10, screw feeder 2 11-1, screw feeder 3 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 feed port 17, return valve 2 18, waste heat boiler 19, steam turbine generator set 20, induced draft fan 21, chimney 22, superheater 2 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, steam drum 36. Detailed implementation manners

[0035] Detailed implementation manner one: As Figure 1 , Figures 3 - 5As shown in the figure, this embodiment discloses a biomass reciprocating grate boiler exhaust gasification power generation coupled with steam gasification hydrogen production device, including a hopper 1, a reciprocating grate gasifier, a screw feeder 1 6, an economizer 7, a superheater 1 8, a primary air preheater 9, a secondary air preheater 10, a screw feeder 2 11-1, a screw feeder 3 11-2, a circulating fluidized bed 12, a high-efficiency cyclone separator 1 13, a high-efficiency cyclone separator 2 14, a differential fluidized bed gasifier 16, a waste heat boiler 19, a steam turbine generator set 20, a superheater 2 23, an air preheater 3 24, a dust collector 25, a high-temperature steam shift reactor (WGS-1) 27, an air preheater 2 28, a low-temperature steam shift reactor (WGS-2) 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 bottom of the reciprocating grate gasifier is provided with a reciprocating grate 2, the side wall of the reciprocating grate gasifier is provided with a secondary air inlet 4, the space from above the reciprocating grate 2 to below the secondary air inlet 4 is a gasification chamber 3, and the space above the secondary air inlet 4 is a secondary combustion chamber 5 (the periphery of the secondary combustion chamber 5 is a membrane water wall); the hopper 1 is a biomass hopper, the discharge port of the hopper 1 is arranged at the front end inlet of the reciprocating grate 2, the primary air preheater 9 is communicated with the lower air chamber of the reciprocating grate 2 through a pipeline, the secondary air inlet 4 is communicated with the secondary air preheater 10 through a pipeline, the flue gas outlet at the top of the secondary combustion chamber 5 is successively communicated with the superheater 1 8, the economizer 7, the primary air preheater 9 and the secondary air preheater 10, and the superheater 1 8, the economizer 7, the primary air preheater 9 and the secondary air preheater 10 are all installed in the tail flue of the reciprocating grate gasifier (the tail flue smoke outlet is communicated with the tail gas treatment system through a pipeline);

[0037] The end of the reciprocating grate 2 is communicated with the biomass carbon feed port 17 of the differential fluidized bed gasifier 16 through a screw feeder 1 6 (which is a biomass carbon screw feeder), the screw feeder 2 11-1 is an auxiliary fuel feeder (the auxiliary fuel is agricultural and forestry biomass), the screw feeder 3 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 ports of the screw feeder 2 11-1 and the screw feeder 3 11-2 are communicated with the circulating fluidized bed 12 (which is an adiabatic combustion chamber). 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 1 13. The discharge port at the lower end of the high-efficiency cyclone separator 1 13 is communicated with the first feed port of the differential fluidized bed gasifier 16 through a return valve 1 15, and the discharge port of the differential fluidized bed gasifier 16 is communicated with the return inlet of the circulating fluidized bed 12 through a return valve 2 18;

[0038] 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 and the high-temperature and high-pressure steam outlet of the reciprocating furnace exhaust gasifier are connected to the steam inlet of the steam turbine generator set 20 through the main pipe 36 (the high-temperature and high-pressure steam generated by the biomass reciprocating furnace exhaust gasification and combustion and the steam generated by the waste heat boiler 19 enter the steam turbine generator set 20 through the main pipe 36 and the steam inlet of the steam turbine generator set 20). The low-pressure cylinder extraction port of the steam turbine generator set 20 (the low-pressure cylinder extracts steam at 0.2 - 0.3 MPa and 200 - 250 °C) is connected to the steam inlet of the superheater 23 through a pipeline. 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;

[0039] 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 gas shift reactor (WGS-1) 27, the air preheater 28, the low-temperature water gas shift reactor (WGS-2) 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. The discharge port at the lower part of the high-efficiency cyclone separator 14 is connected to the second feed inlet at the lower part of the differential fluidized bed gasifier 16.

[0040] 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 (after heating).

[0041] Specific Embodiment 2: As Figure 1 、 Figures 3 - 5 shown (the bed temperature of the differential fluidized bed gasifier 16: 780 - 850 °C), this embodiment discloses a method for biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification to produce hydrogen. The method is implemented based on the device described in Specific Embodiment 1. The method includes the following steps:

[0042] Step 1: Biomass (5 - 40 t / h) in the hopper 1 enters the gasification chamber 3 through the reciprocating grate 2 for gasification. The primary air (preheated by the primary air preheater 9) enters the lower air chamber of the reciprocating grate 2 (the primary air stoichiometric ratio is 0.25 - 0.35). The gas generated in the gasification chamber 3 is mixed with the secondary air (coming from the secondary air preheater 10) and then burns and releases heat in the secondary combustion chamber 5 (the periphery of the secondary combustion chamber 5 is a membrane water wall). The high-temperature flue gas coming out of the secondary combustion chamber 5 successively enters the first superheater 8, the economizer 7, the primary air preheater 9, and the secondary air preheater 10, and then goes to the tail treatment system. The biomass char (1.5 - 12 t / h) discharged from the end of the reciprocating grate 2 is sent into the differential fluidized bed gasifier 16 through the first screw feeder 6. High-temperature steam reacts with the biomass char to produce hydrogen-rich syngas. The second screw feeder 11-1 sends biomass into the circulating fluidized bed 12 for combustion (the biomass quantity satisfies that the outlet temperature of the circulating fluidized bed 12 is 900 - 950 °C, and the feeding quantity is determined by the load). At the same time, the third screw feeder 11-2 sends circulating materials (composed of limestone and dolomite, the mass ratio of limestone to dolomite = 1:1, gradually added at the start of operation, and replenished according to the material loss of the system during normal operation) into the circulating fluidized bed 12 for calcination (the calcination products are used as bed materials on the one hand and as catalysts for the differential fluidized bed gasifier 16 on the other hand).

[0043] 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 chamber, 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 of the flue gas outlet at the top of the circulating fluidized bed 12 carries the circulating materials (calcination products of limestone and dolomite) into the first high-efficiency cyclone separator 13, separates the circulating materials, and sends them into the differential fluidized bed gasifier 16 through the first return valve 15. The biomass char sent into the differential fluidized bed gasifier 16 through the first screw feeder 6 reacts with the fed high-temperature steam at 550 - 600 °C to generate syngas (main components: H2, CO, CO2, CH4) at a bed temperature of 780 - 850 °C.

[0044] Step 2: The high-temperature flue gas coming out of the flue gas outlet at the top of the first high-efficiency cyclone separator 13 enters the waste heat boiler 19. The steam generated by the waste heat boiler 19 converges with the high-temperature and high-pressure steam generated by the biomass reciprocating grate gasification combustion and is sent to the steam turbine generator set 20 for power generation. The extraction steam from the low-pressure cylinder of the steam turbine generator set 20 (steam at 0.2 - 0.3 MPa and a temperature of 200 - 250 °C) enters the second superheater 23 and is heated to 550 - 600 °C, and then enters the differential fluidized bed gasifier 16 from the bottom air chamber of the differential fluidized bed gasifier 16.

[0045] 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. The biomass char reacts with high-temperature steam (steam / biomass char weight ratio = 1 - 3:1) at this temperature to generate syngas H2, CO, CO2, CH4, and trace H2S. The gas production rate of 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 ); Meanwhile, 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) to remove 90% of H2S, and H2S < 10 mg / Nm 3 (meeting the requirement that the subsequent water-gas shift reaction catalyst will not fail);

[0046] Step 4: The high-temperature syngas coming out from the top of the differential fluidized bed gasifier 16 enters the high-efficiency cyclone separator II 14, where the carried circulating material is separated and returned to the differential fluidized bed gasifier 16. Then the syngas is cooled to 300 - 350 °C after passing through the superheater II 23 and the air preheater III 24, and 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 removal efficiency of the dust collector 25 reaches more than 99.9%, and the dust content in the syngas ≤ 5 mg / m 3 ). After dust removal, the syngas (temperature 300 - 350 °C) enters the high-temperature water-gas shift reactor 27 (WGS-1, reaction conditions: commercial catalyst SCST-221, 300 - 350 °C, SV = 1300 - 2700 h -1 ), and after the temperature rises to 380 - 450 °C, it enters the air preheater II 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, reaction conditions: commercial catalyst SCST-231, 190 - 200 °C, SV = 4600 - 5100 h -1), the steam / CO molar ratio ≥ 2, for the high-temperature and low-temperature water-gas shift reactions: CO + H2O = H2 + CO2, the total conversion rate of CO is over 95%; the synthesis gas 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 synthesis gas drops to 120 - 150 °C. Then the synthesis gas 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 synthesis gas (recovering the latent heat of vaporization in the steam to improve the thermal efficiency of the system) and the organic amine scrubber 33 (mature technology) 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. After the organic amine aqueous solution absorbs CO2, it is regenerated (heated to 120 - 150 °C, then CO2 and water vapor are released by analysis, and high-purity CO2 is obtained by condensation and separation to achieve CO2 capture); then the synthesis gas enters the pressure swing adsorption system (PSA) 35 through the compressor 34 to obtain 99.9% H2, and the exhaust gas from the pressure swing adsorption system 35 (containing H2, CO, CO2) is sent to the circulating fluidized bed 12 for combustion to release heat.

[0047] The effect of the second specific implementation manner is as follows: The reciprocating grate 2 is used to gasify to produce biomass carbon, and the biomass carbon is gasified with water vapor at 780 - 850 °C in the differential fluidized bed gasifier 16 to produce H2. At the same time, the fuel gas is burned in the secondary combustion chamber 5 to generate high-temperature and high-pressure steam, which is combined with the steam of the waste heat boiler 19 for power generation, realizing the high-value utilization of biomass; in addition, after using the high-temperature water-gas shift reactor (WSG-1) 27 and the low-temperature water-gas shift reactor (WSG-2) 29, the volume fraction of H2 reaches over 85%. After absorbing CO2 by organic amine, the volume fraction of H2 in the synthesis gas reaches over 90%.

[0048] The third specific implementation manner: As Figure 2 、 Figures 6 - 8 shown, this implementation manner discloses a biomass reciprocating grate exhaust gasification power generation coupled with steam gasification hydrogen production device, including a hopper 1, a reciprocating grate 2, a screw feeder 6, an economizer 7, a superheater 8, a primary air preheater 9, a secondary air preheater 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 steam turbine generator set 20, a superheater 23, an air preheater 24, a dust collector 25, a high-temperature water-gas shift reactor (WGS-1) 27, an air preheater 28, a low-temperature water-gas shift reactor (WGS-2) 29, an air preheater 30, a condenser 32, an organic amine scrubber 33, a compressor 34, and a pressure swing adsorption system (PSA) 35;

[0049] A reciprocating grate 2 is provided at the bottom of the reciprocating grate gasifier. A secondary air inlet 4 is provided on the side wall of the reciprocating grate gasifier. The space from above the reciprocating grate 2 to below the secondary air inlet 4 is the gasification chamber 3, and the space above the secondary air inlet 4 is the secondary combustion chamber 5 (the periphery of the secondary combustion chamber 5 is a membrane water wall). The hopper 1 is a biomass hopper, and the discharge port of the hopper 1 is arranged at the front end inlet of the reciprocating grate 2. The primary air preheater 9 is connected to the lower air chamber of the reciprocating grate 2 through a pipeline (the primary air stoichiometric ratio is 0.25 - 0.35). The secondary air inlet 4 is connected to the secondary air preheater 10 through a pipeline. The flue gas outlet at the top of the secondary combustion chamber 5 is successively connected to the first superheater 8, the economizer 7, the primary air preheater 9, and the secondary air preheater 10. The first superheater 8, the economizer 7, the primary air preheater 9, and the secondary air preheater 10 are all installed in the tail flue of the reciprocating grate gasifier (the flue gas outlet of the tail flue is connected to the tail gas treatment system through a pipeline);

[0050] The end of the reciprocating grate 2 is connected to the biomass charcoal feed port 17 of the differential fluidized bed gasifier 16 through a screw feeder 6 (which is a biomass charcoal 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 consists of limestone, dolomite, and Ni-based catalyst, and the mass ratio of limestone:dolomite:Ni-based catalyst = 1:1:1. The discharge ports of the screw feeder 11-1 and the screw feeder 11-2 are connected to the circulating fluidized bed 12 (which is an adiabatic combustion chamber). The flue gas outlet at the top of the circulating fluidized bed 12 is connected to 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 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 a return valve 15. The discharge port of the differential fluidized bed gasifier 16 is connected to the return inlet of the circulating fluidized bed 12 through a return valve 18;

[0051] 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 and the high-temperature and high-pressure steam outlet of the reciprocating grate gasifier are connected to the steam inlet of the steam turbine generator set 20 through a main pipe 36 (the high-temperature and high-pressure steam generated by the biomass reciprocating grate gasification and combustion and the steam generated by the waste heat boiler 19 enter the steam turbine generator set 20 through the main pipe 36 and the steam inlet of the steam turbine generator set 20). The low-pressure cylinder extraction port of the steam turbine generator set 20 (the low-pressure cylinder extraction is 0.2 - 0.3 MPa, 200 - 250 °C) is connected to the steam inlet of the second superheater 23 through a pipeline. The superheated steam outlet of the second superheater 23 is connected to the superheated steam inlet of the bottom air chamber of the differential fluidized bed gasifier 16;

[0052] 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 II 23. The syngas outlet of the superheater II 23 is successively connected to the air preheater III 24, the dust collector 25, the high-temperature steam reforming reactor 27, the air preheater II 28, the low-temperature steam reforming 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 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.

[0053] 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 enters the waste heat boiler 19 after being heated by the condenser 32.

[0054] Specific Embodiment 4: As Figure 2 , Figures 6 - 8 shown (the bed temperature of the differential fluidized bed gasifier 16: 600 - 700 °C, in-situ CO2 absorption), this embodiment discloses a method for biomass reciprocating grate gasification power generation coupled with steam gasification for hydrogen production. The method is implemented based on the device described in Specific Embodiment 3, and the method includes the following steps:

[0055] Step 1: Biomass (5 - 40 t / h) in the hopper 1 enters the gasification chamber 3 through the reciprocating grate 2 for gasification. The primary air (preheated by the primary air preheater 9) enters the lower air chamber of the reciprocating grate 2 (the primary air stoichiometric ratio is 0.25 - 0.35). The gas generated in the gasification chamber 3 is mixed with the secondary air (coming from the secondary air preheater 10) and then burns and releases heat in the secondary combustion chamber 5 (the periphery of the secondary combustion chamber 5 is a membrane water wall). The high-temperature flue gas coming out of the secondary combustion chamber 5 successively enters the superheater I 8, the economizer 7, the primary air preheater 9, and the secondary air preheater 10, and then goes to the tail treatment system. The biomass char (1.5 - 12 t / h) discharged from the end of the reciprocating grate 2 is sent into the differential fluidized bed gasifier 16 through the screw feeder I 6. High-temperature steam reacts with the biomass char to produce hydrogen-rich syngas. The screw feeder II 11-1 feeds biomass into the circulating fluidized bed 12 for combustion. The biomass quantity is such that the outlet temperature of the circulating fluidized bed 12 is 900 - 950 °C, and the feeding amount is determined by the load. At the same time, the screw feeder III 11-2 feeds the circulating material (composed 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).

[0056] High-temperature air at 300 - 350 °C enters the circulating fluidized bed 12 from the bottom air chamber to assist combustion (the circulating fluidized bed 12 is an adiabatic combustion furnace with a fluidization velocity of 6 - 10 m / s and a circulation ratio of 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 materials (calcination products of limestone, dolomite, and Ni-based catalyst) and enters the high-efficiency cyclone separator I 13. The circulating materials are separated, and a part is sent back into the circulating fluidized bed 12 through the loop seal I 15, and the other part is sent into the differential fluidized bed gasifier 16 through the loop seal I 15;

[0057] Step 2: The high-temperature flue gas coming out 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 combined with the high-temperature and high-pressure steam generated by the biomass reciprocating grate furnace for gasification combustion and is sent to the steam turbine generator set 20 for power generation. The steam extracted from the low-pressure cylinder of the steam turbine generator set 20 (steam at 0.2 - 0.3 MPa and a temperature of 200 - 250 °C) enters the superheater II 23 and is heated to 400 - 450 °C, and then the superheated steam enters the differential fluidized bed gasifier 16 from the bottom air chamber of the differential fluidized bed gasifier 16;

[0058] Step 3: In the differential fluidized bed gasifier 16, the high-temperature circulating materials and high-temperature superheated steam heat the differential fluidized bed gasifier 16 to 600 - 700 °C. The biomass char discharged from the reciprocating grate 2 is sent into the differential fluidized bed gasifier 16 through the screw feeder I 6. The biomass char reacts with high-temperature steam (the weight ratio of steam to biomass char = 1 - 3:1) under the action of a catalyst (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 reaction of CO + H2O = H2 + CO2 (so 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 char is 2.0 - 2.5 Nm 3 / kg; At the same time, CaO reacts with H2S to generate CaS (the reaction time in the differential fluidized bed gasifier 16 is not less than 10 s), removing 90% of H2S, so that H2S in the syngas < 10 mg / Nm 3(Meet the requirement that the subsequent water-gas shift catalyst is not deactivated); The circulating materials containing CaCO3, CaS and the unreacted biochar (accounting for 10-15% of the total biochar weight) enter the circulating fluidized bed 12 through the second return valve 18, causing the decomposition of CaCO3 into CaO and CO2, and the decomposition of CaS into CaO and SO2. After the Ni-based catalyst removes carbon deposition in the circulating fluidized bed 12, it enters the differential fluidized bed gasifier 16 together with CaO and MgO (calcination products of limestone and dolomite) after being separated by the first high-efficiency cyclone separator 13;

[0059] 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 therein 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 second superheater 23 and the third air preheater 24, and then cools down to 300-350 °C and 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 (temperature 300-350 °C) enters the high-temperature water-gas shift reactor 27 (WGS-1, reaction conditions: commercial catalyst SCST-221, 300-350 °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, and the temperature of the syngas drops to 190-200 °C and enters the low-temperature water-gas shift reactor 29 (WGS-2, reaction conditions: 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: the total conversion rate of CO in the reaction CO + H2O = H2 + CO2 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 (a mature existing technology, using the feed water of the waste heat boiler 19 to condense the water vapor in the syngas, recovering the latent heat of vaporization in the steam, and improving the thermal efficiency of the system) and the organic amine scrubber 33 (a mature technology), removing the remaining dust, trace H2S, and over 90% of CO2 in the syngas. The clean syngas temperature 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 (PSA) 35 through the compressor 34 to obtain 99.9% H2, and the exhaust gas from the pressure swing adsorption system 35 (containing H2, CO, CO2) is sent to the circulating fluidized bed 12 for combustion to release heat.

[0060] The effect of the fourth specific embodiment is that the biomass char generated by the gasification of the exhaust gas from the biomass reciprocating furnace enters the differential fluidized bed gasifier 16, where it in-situ absorbs CO2 at 600 - 700 °C, causing the reaction CO + H2O = CO2 + H2 to proceed in the forward direction, the CO2 concentration to drop significantly to less than or equal to 3%, and the H2 concentration to rise 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.

[0061] 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 second blower 31 is connected to the air inlet of the first air preheater 30 through a pipeline, the air outlet of the first air preheater 30 is connected to the air inlet of the second air preheater 28 through a pipeline, and the air outlet of the second air preheater 28 is connected to the air inlet of the third air preheater 24 through a pipeline.

[0062] 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".

[0063] The above are only the preferred specific embodiments 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 of the present invention patent and its inventive concept, makes equivalent substitutions or changes, and should be covered within the protection scope of the present invention patent.

Claims

1. A biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification hydrogen production device, characterized in that: It includes a hopper (1), a reciprocating grate gasifier, a first screw feeder (6), a economizer (7), a first superheater (8), a primary air preheater (9), a secondary air preheater (10), a second screw feeder (11-1), a third screw feeder (11-2), a circulating fluidized bed (12), a first high-efficiency cyclone separator (13), a second high-efficiency cyclone separator (14), a differential fluidized bed gasifier (16), a waste heat boiler (19), a steam turbine generator set (20), a second superheater (23), a third air preheater (24), a dust collector (25), a high-temperature steam reforming reactor (27), a second air preheater (28), a low-temperature steam reforming reactor (29), a first air preheater (30), a condenser (32), an organic amine scrubber (33), a compressor (34) and a pressure swing adsorption system (35); The reciprocating grate gasifier is provided with a reciprocating grate (2) at the bottom, a secondary air inlet (4) on the side wall of the reciprocating grate gasifier. The space from above the reciprocating grate (2) to below the secondary air inlet (4) is the gasification chamber (3), and the space above the secondary air inlet (4) is the secondary combustion chamber (5); the hopper (1) is a biomass hopper, and the discharge port of the hopper (1) is arranged at the front end inlet of the reciprocating grate (2). The primary air preheater (9) is connected to the lower air chamber of the reciprocating grate (2) through a pipeline, the secondary air inlet (4) is connected to the secondary air preheater (10) through a pipeline, and the flue gas outlet at the top of the secondary combustion chamber (5) is successively connected to the first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10). The first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10) are all installed in the tail flue of the reciprocating grate gasifier; the end of the reciprocating grate (2) is connected to the biomass carbon feed port (17) of the differential fluidized bed gasifier (16) through the first screw feeder (6). The second screw feeder (11-1) is an auxiliary fuel feeder, and the third screw feeder (11-2) is a circulating material feeder. The circulating material consists of limestone and dolomite. The discharge ports of the second screw feeder (11-1) and the third 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 connected to 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 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) and the high-temperature and high-pressure steam outlet of the reciprocating grate gasifier are connected to the steam inlet of the steam turbine generator set (20) through the main pipe (36). The low-pressure cylinder extraction port of the steam turbine generator set (20) is connected to the steam inlet of the second superheater (23) through a pipeline. The superheated steam outlet of the second 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 second superheater (23). The syngas outlet of the second 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). 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);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 reciprocating furnace exhaust gasification power generation coupled with steam gasification hydrogen production device according to claim 1, wherein: The feed water outlet of the waste heat boiler (19) is communicated with the feed water inlet of the waste heat boiler (19) through the condenser (32).

3. A method for biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification for hydrogen production, characterized in that: The method is implemented based on the device described in claim 2, and the method includes the following steps: Step 1: Biomass in the hopper (1) enters the gasification chamber (3) through the reciprocating grate (2) for gasification. The primary air is preheated and then enters the lower air chamber of the reciprocating grate (2). The gas generated in the gasification chamber (3) is mixed with the secondary air and then burns and releases heat in the secondary combustion chamber (5); The high-temperature flue gas coming out of the secondary combustion chamber (5) sequentially enters the first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10), and then goes to the tail treatment system; The biomass charcoal discharged from the end of the reciprocating grate (2) is sent into the differential fluidized bed gasifier (16) through the first screw feeder (6), and the high-temperature steam reacts with the biomass charcoal to generate hydrogen-rich syngas; The second screw feeder (11-1) sends the biomass into the circulating fluidized bed (12) for combustion. At the same time, the third screw feeder (11-2) sends the circulating material into the circulating fluidized bed (12) for calcination; The 400-450 °C high-temperature air enters the circulating fluidized bed (12) from the bottom air chamber of the circulating fluidized bed (12) to assist combustion. The 900-950 °C high-temperature flue gas carrying the circulating material comes out from the flue gas outlet at the top of the circulating fluidized bed (12) and enters the first high-efficiency cyclone separator (13) to separate the circulating material, and then is sent into the differential fluidized bed gasifier (16) through the first return valve (15); The biomass charcoal sent into the differential fluidized bed gasifier (16) through the first screw feeder (6) reacts with the 550-600 °C high-temperature steam sent in, and syngas is generated at a bed temperature of 780-850 °C; Step 2: The high-temperature flue gas coming out of the flue gas outlet at the top of the first high-efficiency cyclone separator (13) enters the waste heat boiler (19). The steam generated by the waste heat boiler (19) converges with the high-temperature and high-pressure steam generated by the biomass reciprocating grate gasification combustion, and is sent to the steam turbine generator set (20) for power generation. The extraction steam from the low-pressure cylinder of the steam turbine generator set (20) enters the second superheater (23) and is heated to 550-600 °C, and then enters the differential fluidized bed gasifier (16) from the bottom air chamber 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. The biomass char reacts with the high-temperature steam at this temperature to generate syngas H2, CO, CO2, CH4, and trace amounts of H2S. The mass ratio of steam to biomass char = 1 - 3:1, 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 syngas coming out from the top of the differential fluidized bed gasifier (16) enters the high-efficiency cyclone separator II (14), where the circulating materials carried therein are separated and returned to the differential fluidized bed gasifier (16). Then the syngas is cooled to 300 - 350 °C after passing through the superheater II (23) and the air preheater III (24), and enters the dust collector (25). After dust removal, the syngas enters the high-temperature water vapor shift reactor (27), and after the temperature rises to 380 - 450 °C, it enters the air preheater II (28) to preheat the air to 250 - 300 °C. After the syngas temperature drops to 190 - 200 °C, it enters the low-temperature water vapor shift reactor (29), where the steam / CO molar ratio ≥ 2, and 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 temperature rises to 250 - 260 °C, and then enters the air preheater I (30) to preheat the air from room temperature to 130 - 150 °C. After the syngas temperature drops to 120 - 150 °C, the syngas enters the condenser (32), and the water vapor in the syngas is condensed by the feed water of the waste heat boiler (19) and the organic amine scrubber (33) 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 (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 (12) for combustion to release heat.

4. A biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification hydrogen production device, characterized in that: It includes a hopper (1), a reciprocating grate gasifier, a screw feeder I (6), a economizer (7), a superheater I (8), a primary air preheater (9), a secondary air preheater (10), a screw feeder II (11 - 1), a screw feeder III (11 - 2), a circulating fluidized bed (12), a high-efficiency cyclone separator I (13), a high-efficiency cyclone separator II (14), a differential fluidized bed gasifier (16), a waste heat boiler (19), a steam turbine generator set (20), a superheater II (23), an air preheater III (24), a dust collector (25), a high-temperature water vapor shift reactor (27), an air preheater II (28), a low-temperature water vapor shift reactor (29), an air preheater I (30), a condenser (32), an organic amine scrubber (33), a compressor (34) and a pressure swing adsorption system (35); The reciprocating grate gasifier is provided with a reciprocating grate (2) at the bottom, a secondary air inlet (4) on the side wall of the reciprocating grate gasifier. The space from above the reciprocating grate (2) to below the secondary air inlet (4) is the gasification chamber (3), and the space above the secondary air inlet (4) is the secondary combustion chamber (5). The hopper (1) is a biomass hopper, and the discharge port of the hopper (1) is arranged at the front end inlet of the reciprocating grate (2). The primary air preheater (9) is connected to the lower air chamber of the reciprocating grate (2) through a pipeline. The secondary air inlet (4) is connected to the secondary air preheater (10) through a pipeline. The flue gas outlet at the top of the secondary combustion chamber (5) is successively connected to the first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10). The first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10) are all installed in the tail flue of the reciprocating grate gasifier. The end of the reciprocating grate (2) is connected to the biomass carbon feed port (17) of the differential fluidized bed gasifier (16) through a screw feeder one (6). The screw feeder two (11-1) is an auxiliary fuel feeder, and the screw feeder three (11-2) is a circulating material feeder. The circulating material is composed of limestone, dolomite and Ni-based catalyst. The discharge ports of the screw feeder two (11-1) and the screw feeder three (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 high-efficiency cyclone separator one (13). The discharge port at the lower end of the high-efficiency cyclone separator one (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 a return valve one (15). The discharge port of the differential fluidized bed gasifier (16) is connected to the return inlet of the circulating fluidized bed (12) through a return valve two (18). The flue gas outlet at the top of the high-efficiency cyclone separator one (13) is connected to the flue gas inlet of the waste heat boiler (19). The steam outlet of the waste heat boiler (19) and the high-temperature and high-pressure steam outlet of the reciprocating grate gasifier are connected to the steam inlet of the steam turbine generator set (20) through a main pipe (36). The low-pressure cylinder extraction port of the steam turbine generator set (20) is connected to the steam inlet of the second superheater (23) through a pipeline. The superheated steam outlet of the second superheater (23) is connected to the superheated steam inlet of the bottom air chamber 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 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 II (23). The syngas outlet of the superheater II (23) is successively connected to the air preheater III (24), the dust collector (25), the high-temperature steam reforming reactor (27), the air preheater II (28), the low-temperature steam reforming 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 port at the lower part of the differential fluidized bed gasifier (16).; 5. The biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification hydrogen production device according to claim 4, 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).

6. A method for biomass reciprocating furnace exhaust gasification power generation coupled with steam gasification for hydrogen production, characterized in that: The method is implemented based on the device described in claim 5, and the method includes the following steps: Step 1: Biomass in the hopper (1) enters the gasification chamber (3) through the reciprocating grate (2) for gasification. The primary air is preheated and then enters the air chamber at the lower part of the reciprocating grate (2). The gas generated in the gasification chamber (3) is mixed with the secondary air and then burns and releases heat in the secondary combustion chamber (5). The high-temperature flue gas coming out of the secondary combustion chamber (5) successively enters the first superheater (8), the economizer (7), the primary air preheater (9) and the secondary air preheater (10), and then goes to the tail treatment system. The biomass char discharged from the end of the reciprocating grate (2) is sent into the differential fluidized bed gasifier (16) through the first screw feeder (6). High-temperature steam reacts with the biomass char to produce hydrogen-rich syngas. The second screw feeder (11-1) sends the biomass into the circulating fluidized bed (12) for combustion, and the amount of biomass is such that the outlet temperature of the circulating fluidized bed (12) is 900 - 950 °C. At the same time, the third screw feeder (11-2) sends the circulating material into the circulating fluidized bed (12) for calcination. 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 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 first high-efficiency cyclone separator (13) to separate the circulating material. Part of it is sent back into the circulating fluidized bed (12) through the first return valve (15), and the other part is sent into the differential fluidized bed gasifier (16) through the first return valve (15). Step 2: The high-temperature flue gas coming out of the flue gas outlet at the top of the first high-efficiency cyclone separator (13) enters the waste heat boiler (19). The steam generated by the waste heat boiler (19) is combined with the high-temperature and high-pressure steam generated by the gasification and combustion of the biomass reciprocating grate and is sent together into the steam turbine generator set (20) for power generation. The extraction steam from the low-pressure cylinder of the steam turbine generator set (20) enters the second superheater (23) and is heated to 400 - 450 °C. Then, the superheated steam enters the differential fluidized bed gasifier (16) from the air chamber at 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 reciprocating grate (2) is fed into the differential fluidized bed gasifier (16) through the first screw feeder (6). The biomass char reacts with the high-temperature steam 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 generate CaCO3, promoting the forward progress of CO + H2O = H2 + CO2; at the same time, CaO reacts with H2S to generate CaS, removing 90% of H2S, such that H2S in the syngas < 10 mg / Nm 3 ; the mass ratio of steam to biomass char = 1 - 3:1, and the gas production rate of biomass char is 2.0 - 2.5 Nm 3 / kg; 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 enters the differential fluidized bed gasifier (16) together with CaO and MgO after being separated by the first high-efficiency cyclone separator (13); 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 therein 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 II (23) and the air preheater III (24), and then cools down to 300 - 350 °C and enters the dust collector (25). The dust-removed 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. The temperature of the syngas drops to 190 - 200 °C and enters the low-temperature steam reforming reactor (29), with the 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 syngas 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, and the temperature of the syngas drops to 120 - 150 °C. Then the syngas enters the condenser (32) and the organic amine scrubber (33) to remove the remaining dust, trace H2S and over 90% of CO2 in the syngas. The clean syngas cools down 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 (12) for combustion to release heat.

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