CN209957715U

CN209957715U - Biomass pyrolysis gasification hydrogen production system

Info

Publication number: CN209957715U
Application number: CN201920742504.9U
Authority: CN
Inventors: 武超; 肖芳; 张冲
Original assignee: China Shipping Heavy Industry Shanghai New Energy Co Ltd
Current assignee: China Shipping Heavy Industry Shanghai New Energy Co Ltd
Priority date: 2019-05-22
Filing date: 2019-05-22
Publication date: 2020-01-17
Anticipated expiration: 2029-05-22

Abstract

The utility model provides a biomass pyrolysis gasification hydrogen manufacturing system in biomass hydrogen manufacturing technical field, includes biomass storehouse, biomass preheater, screw conveyer, pyrolytic reaction ware, gasification reactor, heat exchanger, soft water storage tank, delivery pump, oxygen storage tank, return water jar, preheats the circulating pipe, and biomass preheater, return water jar, soft water storage tank, delivery pump, third heat exchanger concatenate together through preheating the circulating pipe in proper order, and first heat exchanger, second heat exchanger, third heat exchanger concatenate on gasification gas output tube in proper order. The system is divided into four parts: biomass preheating feeding, biomass pyrolysis, pyrolysis gas gasification and gasification gas waste heat utilization. The utility model has reasonable design and simple process structure; the pyrolysis equipment and the gasification equipment with special structures are adopted to improve the utilization rate of biomass, and special decoking equipment is not needed, so that the generation of tar can be effectively reduced, and the corrosion of the equipment and a pipeline is avoided.

Description

Biomass pyrolysis gasification hydrogen production system

Technical Field

The utility model relates to a pyrolysis gasification system in the technical field of hydrogen production, in particular to a biomass pyrolysis gasification hydrogen production system capable of reducing tar production.

Background

With the rapid development of economy and the continuous increase of population, the consumption of energy by human society is increasing dramatically. At present, fossil fuels still dominate the energy market, accounting for about 87% of the global energy consumption. However, due to the limited reserves of fossil fuels and the generation of a large amount of greenhouse gas CO2 after the combustion of fossil fuels, a series of environmental problems are caused, and people have to look at the development and utilization of clean energy and renewable energy. Among all the alternative energy sources, hydrogen energy is the cleanest energy source on the earth, and the combustion product is water, so that zero emission of pollutants can be really realized. Secondly, the combustion heat value of the hydrogen is as high as 142.3MJ/Kg, which is 3 times of that of the gasoline with the same quality. Therefore, hydrogen has good development prospect as clean, efficient and renewable energy.

At present, the industrial hydrogen production methods mainly comprise an electrolytic water method, a methanol steam reforming method, a heavy oil and natural gas steam catalytic conversion method and the like. The water electrolysis method consumes a large amount of electric energy and has high hydrogen production cost. Methanol steam reforming is the most economical hydrogen production method at present, but a large amount of fossil fuel is consumed in the hydrogen production process, the hydrogen production process is not renewable, and a large amount of CO2 is generated, so that the environment is greatly influenced. With the increasing prominence of the problems of energy shortage, environmental pollution and the like, the use of hydrogen is rapidly increased, and the development of an efficient hydrogen production technology becomes a major problem to be solved urgently in the current society.

Disclosure of Invention

The utility model discloses to prior art's not enough, provide a living beings pyrolysis gasification hydrogen manufacturing system, not only solved the problem that traditional living beings chemistry hydrogen manufacturing is inefficient, hydrogen content is low in the synthetic gas, but also solved the problem that living beings chemistry hydrogen manufacturing power consumption is big, system's thermal efficiency is low.

The utility model is realized by the following technical proposal, the utility model comprises a biomass bin, a biomass preheater, a spiral conveying device, a pyrolysis reactor, a gasification reactor, a first heat exchanger, a second heat exchanger, a third heat exchanger, a soft water storage tank, a conveying pump, an oxygen storage tank, a water return tank, a preheating circulating pipe, a discharging pipe, a conveying pipe, a gasification gas output pipe, a water supply pipe, a steam pipe, a first oxygen supply pipe, a second oxygen supply pipe, a first control valve and a second control valve; the filtering baffle is arranged in the pyrolysis reactor, the front end of the filtering baffle is a first pyrolysis chamber, the rear end of the filtering baffle is a second pyrolysis chamber, and the lower end of the filtering baffle is connected with the residual carbon cache tank through an ash discharge port; the gas inlet, the oxygen inlet and the steam inlet are arranged at the upper end of the pyrolysis reactor, the catalytic filtering carbon layer is arranged in the middle of the pyrolysis reactor, the flow guide device is obliquely arranged between the catalytic filtering carbon layer and the inner wall surface of the pyrolysis reactor, and the gas outlet is arranged at the lower end of the pyrolysis reactor; the biomass preheater, the water return tank, the soft water storage tank, the delivery pump and the third heat exchanger are sequentially connected in series through a preheating circulating pipe; one end of the discharge pipe is connected with a discharge port of the biomass bin, and the other end of the discharge pipe is connected with a feeding port of the biomass preheater; one end of the conveying pipe is connected with a discharge port of the biomass preheater, a feed port of a spiral conveying device at the other end of the conveying pipe is connected, a discharge port of the spiral conveying device is connected with a feed port of a first pyrolysis chamber of the pyrolysis reactor, and a gas outlet of a second pyrolysis chamber of the pyrolysis reactor is connected with a gas inlet of the gasification reactor; the inlet of the gasification gas output pipe is connected with the gas outlet of the gasification reactor, and the first heat exchanger, the second heat exchanger and the third heat exchanger are sequentially connected on the gasification gas output pipe in series; one end of the water supply pipe is connected with a preheating circulating pipe between the third heat exchanger and the delivery pump, and the other end of the water supply pipe is connected with a water inlet of the first heat exchanger; one end of the steam pipe is connected with the air outlet of the first heat exchanger, and the other end of the steam pipe is connected with the steam inlet of the gasification reactor; one end of the first oxygen conveying pipe is connected with the oxygen storage tank, and the other end of the first oxygen conveying pipe is connected with an oxygen inlet of the second heat exchanger; one end of the second oxygen conveying pipe is connected with an oxygen outlet of the second heat exchanger, and the other end of the second oxygen conveying pipe is connected with an oxygen inlet of the gasification reactor; the first control valve and the second control valve are respectively arranged on the water supply pipe and the first oxygen supply pipe.

Further, the utility model discloses in, living beings pre-heater, first heat exchanger, second heat exchanger, third heat exchanger are tubular heat exchanger.

Furthermore, in the utility model discloses in, filter baffle is the metal fiber felt material, the catalysis filters the charcoal layer and is nickel base wholeness catalyst.

The specific process of the utility model is as follows:

firstly, biomass is preheated and fed, namely, a biomass raw material is output from a feed inlet of a biomass bin, preheated by a biomass preheater and sent into a pyrolysis reactor by a spiral conveying device;

and secondly, biomass pyrolysis, namely pyrolyzing the biomass entering the pyrolysis reactor in a first pyrolysis reaction chamber, filtering residues such as charcoal and the like generated by pyrolysis through a filtering baffle plate, discharging the residues to a carbon residue cache tank through an ash discharge port, allowing pyrolysis gas to pass through the filtering baffle plate and enter a second pyrolysis reaction chamber for continuous pyrolysis, and allowing a pyrolysis gas outlet end to be connected with a fuel gas inlet of the gasification reactor and enter the gasification reactor.

Thirdly, gasifying pyrolysis gas: the pyrolysis gas enters the gasification reactor, and gas-phase combustion occurs in the upper space of the gasification furnace, so that tar in the pyrolysis gas is fully cracked. Oxygen and water vapor are heated by the first heat exchanger and the second heat exchanger respectively and then enter the upper part of the reactor through the oxygen inlet and the water vapor inlet to provide a reflecting atmosphere. The partially oxidized gas passes through the catalytic filtering carbon layer to generate reduction reaction, and high-heat-value combustible gas is generated and discharged from a gas outlet under the action of the flow guide device.

Fourthly, gasification gas waste heat utilization: the temperature of a fuel gas outlet is 800 ℃, and a large amount of waste heat can be utilized, so that the first heat exchanger, the second heat exchanger and the third heat exchanger are arranged, and the heat is fully utilized. The gasified fuel gas passes through the three heat exchangers in sequence, and is heated to supply water to produce steam, oxygen-enriched gas and water as heat sources for biomass preheating, and then enters the back-end process. The feed water is pressurized by a delivery pump from the soft water storage tank and respectively enters the first heat exchanger and the third heat exchanger for heating; the feed water passing through the third heat exchanger enters the biomass preheater to preheat the raw material, the condensed water enters the water return tank to be recycled, and the whole system only needs to supplement a small amount of feed water. The oxygen-enriched gas enters a second heat exchanger to be heated and conveyed to an oxygen inlet to enter a gasification reactor.

Compared with the prior art, the utility model discloses have following beneficial effect and do: the utility model has reasonable design and simple process structure; the pyrolysis equipment and the gasification equipment with special structures are adopted to improve the utilization rate of biomass, and special decoking equipment is not needed, so that the generation of tar (the content of tar in combustible gas is less than 5mg/m3) can be effectively reduced, and the corrosion of the equipment and pipelines is avoided. The system has reasonable equipment arrangement and high system thermal efficiency, reduces the emission of environmental pollutants, obviously improves the hydrogen production efficiency, and ensures that the volume fraction of H2 in the gasified fuel gas can reach 45-65 percent.

Drawings

Fig. 1 is a schematic structural view of the present invention;

wherein: 1. biomass bin, 2, biomass preheater, 3, screw conveyer, 4, pyrolysis reactor, 41, first pyrolysis chamber, 42, second pyrolysis chamber, 43, filtering baffle, 44, ash discharge port, 45, carbon residue buffer tank, 5, gasification reactor, 51, gas inlet, 52, oxygen inlet, 53, water vapor inlet, 54, catalytic filtering carbon layer, 55, diversion device, 56, gas outlet, 6, first heat exchanger, 7, second heat exchanger, 8, third heat exchanger, 9, soft water storage tank, 10, delivery pump, 11, oxygen storage tank, 12, water return tank, 13, preheating circulation pipe, 14, discharge pipe, 15, delivery pipe, 16, gasification gas output pipe, 17, water supply pipe, 18, steam pipe, 19, first oxygen supply pipe, 20, second oxygen supply pipe, 21, first control valve, 22, second control valve.

Detailed Description

The embodiments of the present invention will be described in detail with reference to the accompanying drawings, and the embodiments of the present invention are based on the technical solution of the present invention and provide detailed embodiments and specific operation processes, but the scope of the present invention is not limited to the following embodiments.

Examples

As shown in fig. 1, the utility model comprises a biomass bin 1, a biomass preheater 2, a spiral conveying device 3, a pyrolysis reactor 4, a gasification reactor 5, a first heat exchanger 6, a second heat exchanger 7, a third heat exchanger 8, a soft water storage tank 9, a conveying pump 10, an oxygen storage tank 11, a return water tank 12, a preheating circulating pipe 13, a discharging pipe 14, a conveying pipe 15, a gasified fuel gas output pipe 16, a water supply pipe 17, a steam pipe 18, a first oxygen supply pipe 19, a second oxygen supply pipe 20, a first control valve 21 and a second control valve 22; the filtering baffle 43 is arranged in the pyrolysis reactor 4, the front end of the filtering baffle 43 is a first pyrolysis chamber 41, the rear end of the filtering baffle 43 is a second pyrolysis chamber 42, and the lower end of the filtering baffle 43 is connected with a residual carbon cache tank 45 through an ash discharge port 44; the gas inlet 51, the oxygen inlet 52 and the water vapor inlet 53 are arranged at the upper end of the pyrolysis reactor 4, the catalytic filtering carbon layer 54 is arranged at the middle part of the pyrolysis reactor 4, the flow guide device 55 is obliquely arranged between the catalytic filtering carbon layer 54 and the inner wall surface of the pyrolysis reactor 4, and the gas outlet 56 is arranged at the lower end of the pyrolysis reactor 4; the biomass preheater 2, the water return tank 12, the soft water storage tank 9, the delivery pump 10 and the third heat exchanger 8 are sequentially connected in series through a preheating circulating pipe 13; one end of the discharge pipe 14 is connected with a discharge hole of the biomass bin 1, and the other end of the discharge pipe 14 is connected with a feeding hole of the biomass preheater 2; one end of the conveying pipe 15 is connected with a discharge port of the biomass preheater 2, the other end of the conveying pipe 15 is connected with a feed port of the spiral conveying device 3, a discharge port of the spiral conveying device 3 is connected with a feed port of the first pyrolysis chamber 41 of the pyrolysis reactor 4, and a fuel gas outlet of the second pyrolysis chamber 42 of the pyrolysis reactor 4 is connected with a fuel gas inlet 51 of the gasification reactor 5; the inlet of the gasified fuel gas output pipe 16 is connected with the fuel gas outlet 56 of the gasification reactor 5, and the first heat exchanger 6, the second heat exchanger 7 and the third heat exchanger 8 are sequentially connected on the gasified fuel gas output pipe 16 in series; one end of a water supply pipe 17 is connected with the preheating circulating pipe 13 between the third heat exchanger 8 and the delivery pump 10, and the other end of the water supply pipe 17 is connected with the water inlet of the first heat exchanger 6; one end of the steam pipe 18 is connected with the air outlet of the first heat exchanger 6, and the other end of the steam pipe 18 is connected with the steam inlet 53 of the gasification reactor 5; one end of the first oxygen conveying pipe 19 is connected with the oxygen storage tank 11, and the other end of the first oxygen conveying pipe 19 is connected with an oxygen inlet of the second heat exchanger 7; one end of the second oxygen pipe 20 is connected with the oxygen outlet of the second heat exchanger 7, and the other end of the second oxygen pipe 20 is connected with the oxygen inlet 52 of the gasification reactor 5; the first control valve 21 and the second control valve 22 are respectively arranged on the water supply pipe 17 and the first oxygen supply pipe 19. The biomass preheater 2, the first heat exchanger 6, the second heat exchanger 7 and the third heat exchanger 8 are all tube type heat exchangers. The filtering baffle 43 is made of metal fiber felt material, and the catalytic filtering carbon layer 54 is a nickel-based monolithic catalyst.

The utility model discloses an implementation as follows:

firstly, biomass raw materials are output from a feeding port of a biomass bin 1, preheated by a biomass preheater 2 and sent into a pyrolysis reactor 4 by a spiral conveying device 3; wherein the biomass feedstock may be: agricultural and forestry crops such as fruit peel and straw; the biomass preheater 2 is a tubular heat exchanger.

Secondly, the biomass entering the pyrolysis reactor 4 is firstly pyrolyzed in the first pyrolysis reaction chamber 41, residues such as charcoal generated by pyrolysis are filtered by the filtering baffle 43 and then discharged to the carbon residue buffer tank 45 through the ash discharge port 44, the pyrolysis gas passes through the filtering baffle 43 and enters the second pyrolysis reaction chamber 42 for continuous pyrolysis, and the outlet end of the pyrolysis gas is connected with the gas inlet 51 of the gasification reactor 5 and enters the gasification reactor 5. Wherein the pyrolysis temperature of the first pyrolysis reaction chamber 41 is 600-700 ℃, and the pyrolysis temperature of the second pyrolysis reaction chamber 42 is 1100-1200 ℃; the filtering baffle 43 is made of metal fiber felt material; the residual carbon in the residual carbon cache tank 45 can be simply treated to prepare biomass carbon;

thirdly, the pyrolysis gas enters the gasification reactor 5, and gas phase combustion occurs in the upper space of the gasification furnace, so that tar in the pyrolysis gas is fully cracked. Oxygen and water vapor are heated by the first heat exchanger 6 and the second heat exchanger 7 respectively and then enter the upper part of the reactor through the oxygen inlet 52 and the water vapor inlet 53 to provide a reflecting atmosphere. The partially oxidized gas passes through the catalytic filter carbon layer 54 to undergo a reduction reaction, so as to generate high-heat-value combustible gas, and the combustible gas is discharged from the gas outlet 56 under the action of the flow guide device 55. Wherein the gas phase combustion space ensures that the temperature is more than 1100 ℃, and the temperature of a gas outlet is 800 ℃; the catalytic filtering carbon layer 54 is a nickel-based monolithic catalyst, and because tar in the gas is fully cracked, the content of the carried catalyst is very low, so that the requirements of subsequent application can be met, and the cost is greatly saved. The flow rates of the water vapor and the oxygen gas into the gasification reactor 5 can be controlled by the first control valve 21 and the second control valve 22.

Fourthly, the temperature of a fuel gas outlet is 800 ℃, and a large amount of waste heat can be utilized, so that the first heat exchanger 6, the second heat exchanger 7 and the third heat exchanger 8 are arranged, and the heat is fully utilized. The gasified fuel gas passes through the three heat exchangers in sequence, the gasified fuel gas is heated to supply water to produce steam, the oxygen-enriched gas is heated, the heated water supply is used as a heat source for preheating the biomass, and then the biomass enters the back-end process. The feedwater gets into first heat exchanger 6 and third heat exchanger 8 respectively from soft water storage tank 9 through the pressure boost of delivery pump 10 and heats, and the feedwater through third heat exchanger 8 gets into biomass preheater 2 and preheats the raw materials, and the condensate water gets into return water jar 12, recycles, and entire system only need supply a small amount of feedwater can. The oxygen-enriched gas enters the second heat exchanger 7 to be heated and delivered to the oxygen inlet 52 to enter the gasification reactor 5. The first heat exchanger 6, the second heat exchanger 7 and the third heat exchanger 8 can be tubular heat exchangers; the flow rate of the water vapor is 0.8-1.5g/min, and the maximum hydrogen production rate is 102 g/kg; the overall thermal efficiency of the system reaches 96 percent; the volume fraction of H2 in the gasified fuel gas is 45-65%, which is improved by about 20% compared with the prior art.

The foregoing description of the specific embodiments of the invention has been presented. It is to be understood that the present invention is not limited to the specific embodiments described above, and that various changes and modifications may be made by those skilled in the art within the scope of the appended claims without departing from the spirit of the invention.

Claims

1. A biomass pyrolysis gasification hydrogen production system is characterized by comprising a biomass bin (1), a biomass preheater (2), a spiral conveying device (3), a pyrolysis reactor (4), a gasification reactor (5), a first heat exchanger (6), a second heat exchanger (7), a third heat exchanger (8), a soft water storage tank (9), a conveying pump (10), an oxygen storage tank (11), a water return tank (12), a preheating circulating pipe (13), a discharge pipe (14), a conveying pipe (15), a gasification gas output pipe (16), a water supply pipe (17), a steam pipe (18), a first oxygen supply pipe (19), a second oxygen supply pipe (20), a first control valve (21) and a second control valve (22); the filtering baffle (43) is arranged in the pyrolysis reactor (4), the front end of the filtering baffle (43) is a first pyrolysis chamber (41), the rear end of the filtering baffle (43) is a second pyrolysis chamber (42), and the lower end of the filtering baffle (43) is connected with a residual carbon cache tank (45) through an ash discharge port (44); the gas inlet (51), the oxygen inlet (52) and the steam inlet (53) are arranged at the upper end of the pyrolysis reactor (4), the catalytic filtering carbon layer (54) is arranged in the middle of the pyrolysis reactor (4), the flow guide device (55) is obliquely arranged between the catalytic filtering carbon layer (54) and the inner wall surface of the pyrolysis reactor (4), and the gas outlet (56) is arranged at the lower end of the pyrolysis reactor (4); the biomass preheater (2), the return water tank (12), the soft water storage tank (9), the delivery pump (10) and the third heat exchanger (8) are sequentially connected in series through a preheating circulating pipe (13); one end of the discharge pipe (14) is connected with a discharge hole of the biomass bin (1), and the other end of the discharge pipe (14) is connected with a feeding hole of the biomass preheater (2); one end of the conveying pipe (15) is connected with a discharge hole of the biomass preheater (2), a feeding hole of the spiral conveying device (3) at the other end of the conveying pipe (15) is connected, a discharge hole of the spiral conveying device (3) is connected with a feeding hole of a first pyrolysis chamber (41) of the pyrolysis reactor (4), and a gas outlet of a second pyrolysis chamber (42) of the pyrolysis reactor (4) is connected with a gas inlet (51) of the gasification reactor (5); the inlet of the gasified fuel gas output pipe (16) is connected with the fuel gas outlet (56) of the gasification reactor (5), and the first heat exchanger (6), the second heat exchanger (7) and the third heat exchanger (8) are sequentially connected on the gasified fuel gas output pipe (16) in series; one end of a water supply pipe (17) is connected with a preheating circulating pipe (13) between the third heat exchanger (8) and the delivery pump (10), and the other end of the water supply pipe (17) is connected with a water inlet of the first heat exchanger (6); one end of the steam pipe (18) is connected with the air outlet of the first heat exchanger (6), and the other end of the steam pipe (18) is connected with the steam inlet (53) of the gasification reactor (5); one end of the first oxygen conveying pipe (19) is connected with the oxygen storage tank (11), and the other end of the first oxygen conveying pipe (19) is connected with an oxygen inlet of the second heat exchanger (7); one end of the second oxygen conveying pipe (20) is connected with an oxygen outlet of the second heat exchanger (7), and the other end of the second oxygen conveying pipe (20) is connected with an oxygen inlet (52) of the gasification reactor (5); the first control valve (21) and the second control valve (22) are respectively arranged on the water supply pipe (17) and the first oxygen supply pipe (19).

2. The biomass pyrolysis gasification hydrogen production system according to claim 1, wherein the biomass preheater (2), the first heat exchanger (6), the second heat exchanger (7) and the third heat exchanger (8) are all tubular heat exchangers.

3. The biomass pyrolysis gasification hydrogen production system according to claim 1, wherein the filtering baffle (43) is a metal fiber felt material, and the catalytic filtering carbon layer (54) is a nickel-based monolithic catalyst.