System for preparing green methanol and co-producing green ammonia by gasifying and oxidizing biomass with air

Abstract

The utility model discloses a system for producing green methanol and co-producing green ammonia by gasifying and oxidizing biomass by using air, which comprises a biomass gasifier, a first group of dust removal heat exchangers and a synthesis gas oxidizing furnace, the output end of the synthesis gas oxidation furnace is sequentially connected with a second group of dust removal heat exchangers, a primary purification system, a secondary purification system and a carbon dioxide and nitrogen storage cabinet, and the output end of the carbon dioxide and nitrogen storage cabinet is connected with a carbon dioxide and nitrogen separator; the output end of the carbon dioxide and nitrogen separator is connected with a carbon dioxide storage cabinet and a nitrogen storage cabinet, and the output ends of the carbon dioxide storage cabinet and the nitrogen storage cabinet are connected with a green methanol catalytic synthesis reactor and a green ammonia catalytic synthesis reactor. According to the utility model, the combustible gas part in the high-temperature synthesis gas is completely oxidized and converted into carbon dioxide and water, and gaseous tar is converted into carbon dioxide and water in the complete oxidation process, so that the total amount of carbon dioxide is increased, and the cost in the tar removal process is saved.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of biomass energy utilization technology, specifically to a system for producing green methanol and green ammonia by air gasification and oxidation of biomass. BACKGROUND

[0002] Biomass energy is the fourth largest resource on earth, second only to coal, oil and natural gas, and is also the largest renewable energy resource. Biomass has the characteristics of wide distribution, abundant reserves, renewability, low pollution, etc. and is one of the most potential fossil energy alternative energy sources. At present, the energy utilization methods of biomass energy mainly include fermentation to produce fuel, biogas, gasification, fast pyrolysis and carbonization.

[0003] In the process of pyrolyzing biomass raw materials, the biomass gasifier initially produces high-temperature gas, with a furnace temperature of 700-800 degrees Celsius, and the gas contains tar (the tar at this time is in a gaseous state). In order to effectively use this green gas to replace petrochemical fuels, the high-temperature gas needs to be cooled to room temperature before being delivered to user equipment through a pipeline.

[0004] When using the biomass gasification produced by the biomass gasification furnace to synthesize green methanol, the biomass synthesis gas needs to be deeply treated. Since the biomass gasification synthesis gas of the prior art contains tar, tar needs to be removed during the purification process. In addition, the boiling points of carbon monoxide and nitrogen are close, so the separation is difficult and the cost is high.

[0005] Moreover, before the purification of the high-temperature synthesis gas of the biomass gasification, the synthesis gas contains gaseous tar. With the water washing and temperature reduction, the tar will condense and mix with the sewage. To remove these liquid tar from the sewage, a certain amount of purification cost needs to be increased. SUMMARY

[0006] The utility model aims at providing a system for producing green methanol and green ammonia by air gasification and oxidation of biomass to solve the problems raised in the background.

[0007] In order to solve the above technical problems, the utility model provides technical scheme as follows: A system for producing green methanol and green ammonia by air gasification and oxidation of biomass, comprising a biomass gasifier, an exhaust end of the biomass gasifier being connected to an air inlet end of a first set of dust removal heat exchangers through a pipeline, an air outlet end of the first set of dust removal heat exchangers being connected to an input end of a high-temperature fan through a pipeline, an output end of the high-temperature fan being connected to a synthesis gas oxidation furnace, an output end of the synthesis gas oxidation furnace being connected to a second set of dust removal heat exchangers, an output end of the second set of dust removal heat exchangers being connected to a primary purification system and a secondary purification system in sequence through a pipeline, an output end of the secondary purification system being connected to a carbon dioxide and nitrogen gas storage tank through a Roots blower, an output end of the carbon dioxide and nitrogen gas storage tank being connected to a carbon dioxide and nitrogen gas separator, output ends of the carbon dioxide and nitrogen gas separator being connected to a carbon dioxide storage tank and a nitrogen gas storage tank respectively through a pipeline, and output ends of the carbon dioxide storage tank and the nitrogen gas storage tank being connected to a green methanol catalytic synthesis reactor and a green ammonia catalytic synthesis reactor respectively, input ends of the green methanol catalytic synthesis reactor and the green ammonia catalytic synthesis reactor being connected to a green hydrogen storage tank through a pipeline, and output ends of the green methanol catalytic synthesis reactor and the green ammonia catalytic synthesis reactor being connected to a green methanol storage tank and a green ammonia storage tank respectively.

[0008] In a preferred embodiment, the first set of dust removal heat exchangers and the second set of dust removal heat exchangers are both two-stage cyclone dust removal heat exchangers, which have good dust removal and heat exchange effects on high-temperature flue gas.

[0009] In a preferred embodiment, the waste heat of the first set of dust removal heat exchangers, the second set of dust removal heat exchangers and the synthesis gas oxidation furnace is recovered for heat-electricity-cold supply and cooling of the carbon dioxide and nitrogen gas separator, so that heat can be recycled and energy consumption can be saved.

[0010] In a preferred embodiment, the primary purification system is spray water washing dust removal, electrostatic dust removal or air cooling dust removal, and the secondary purification system is filter filtration and activated carbon adsorption.

[0011] In a preferred embodiment, the carbon dioxide and nitrogen gas separator is a pressure swing adsorption separator, a membrane separator or a low-temperature deep cooling separator.

[0012] In a preferred embodiment, green hydrogen is added to the green methanol catalytic synthesis reactor to synthesize green methanol, and green hydrogen is added to the green ammonia catalytic synthesis reactor to synthesize green ammonia.

[0013] Compared with the prior art, the utility model has the advantages of:

[0014] 1. The utility model discloses after the biomass gasification, the combustible gas part (carbon monoxide, hydrogen, methane) of high -temperature synthesis gas is through complete oxidation system, and the combustible gas part of synthesis gas is completely oxidized, and the nitrogen in synthesis gas does not participate in the reaction, and finally obtained the mixed gas of carbon dioxide and nitrogen, and the separation cost of carbon dioxide and nitrogen is relatively low, and then reduce the cost of producing green methanol.

[0015] 2. The utility model discloses before the high -temperature synthesis gas purification, the combustible gas part in high -temperature synthesis gas is completely oxidized and is converted into carbon dioxide and water, and gaseous tar will be converted into carbon dioxide and water in the complete oxidation process, and this increases the total amount of carbon dioxide, and the cost and expense in the process of removing tar are saved.

[0016] 3. The utility model discloses using air as the gasification agent of gasification furnace and using air as the gasification agent of complete oxidation system, and the cost is lowest, and using air as the gasification agent, after the nitrogen in synthesis gas is separated from carbon dioxide, nitrogen and green hydrogen synthesis green ammonia also have very good economic value. DRAWINGS

[0017] The drawings are used to provide further understanding of the utility model and constitute part of the specification, and are used to explain the utility model along with the embodiments of the utility model, and do not constitute the limitation to the utility model. In the drawings:

[0018] Figure 1 It is the system structure schematic diagram of the utility model.

[0019] In the drawing: 1, biomass gasification furnace;2, first group dust removal heat exchanger;3, high -temperature fan;4, synthesis gas oxidation furnace;5, second group dust removal heat exchanger;6, primary purification system;7, secondary purification system;8, Roots blower;9, carbon dioxide and nitrogen storage tank;10, carbon dioxide and nitrogen separator;11, green methanol catalytic synthesis reactor;12, green ammonia catalytic synthesis reactor;13, carbon dioxide storage tank;14, nitrogen storage tank;15, green methanol storage tank;16, green ammonia storage tank. DETAILED DESCRIPTION

[0020] The technical scheme in the embodiments of the utility model will be clearly and completely described below in conjunction with the drawings in the embodiments of the utility model, and obviously, the described embodiments are only a part of the embodiments of the utility model, not all the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by the ordinary skill in the art without creative labor belong to the scope of the utility model protection.

[0021] Please refer to Figure 1The utility model provides a kind of system for green methanol and green ammonia co-production with air gasification and oxidation biomass, including biomass gasifier 1, the gas exhaust end of the biomass gasifier 1 is connected with the air inlet end of first group dust removal heat exchanger 2 by pipeline, the gas exhaust end of the first group dust removal heat exchanger 2 is connected with the input end of high-temperature fan 3 by pipeline, the output end of the high-temperature fan 3 is connected with synthetic gas oxidation furnace 4, the output end of the synthetic gas oxidation furnace 4 is connected with second group dust removal heat exchanger 5, the output end of the second group dust removal heat exchanger 5 is sequentially connected with primary purification system 6 and secondary purification system 7 by pipeline, the output end of the secondary purification system 7 is connected with carbon dioxide and nitrogen gas storage tank 9 by Roots blower 8, the output end of the carbon dioxide and nitrogen gas storage tank 9 is connected with carbon dioxide and nitrogen gas separator 10, the output end of the carbon dioxide and nitrogen gas separator 10 is respectively connected with carbon dioxide storage tank 13 and nitrogen gas storage tank 14 by pipeline, the output end of the carbon dioxide storage tank 13 and nitrogen gas storage tank 14 is connected with green methanol catalytic synthesis reactor 11 and green ammonia catalytic synthesis reactor 12 respectively, the input end of the green methanol catalytic synthesis reactor 11 and green ammonia catalytic synthesis reactor 12 is connected with green hydrogen storage tank by pipeline, the output end of the green methanol catalytic synthesis reactor 11 and green ammonia catalytic synthesis reactor 12 is connected with green methanol storage tank 15 and green ammonia storage tank 16 respectively.

[0022] In a preferred embodiment, the first group dust removal heat exchanger 2 and the second group dust removal heat exchanger 5 both adopt two-stage cyclone dust removal heat exchanger.

[0023] In a preferred embodiment, the waste heat of the first group dust removal heat exchanger 2, the second group dust removal heat exchanger 5 and the synthetic gas oxidation furnace 4 is recovered for heat and power supply and cooling supply of the carbon dioxide and nitrogen gas separator 10.

[0024] In a preferred embodiment, the primary purification system 6 is spray water washing dust removal, electrostatic dust removal or air cooling dust removal, and the secondary purification system 7 is filter filtration and activated carbon adsorption.

[0025] In a preferred embodiment, the carbon dioxide and nitrogen gas separator 10 is pressure swing adsorption separation, membrane separation or low-temperature cryogenic separation.

[0026] In a preferred embodiment, green hydrogen is added in the green methanol catalytic synthesis reactor 11 to synthesize green methanol, and green hydrogen is added in the green ammonia catalytic synthesis reactor 12 to synthesize green ammonia.

[0027] The working principle of the utility model:

[0028] When in use, the biomass fuel is sent into the biomass gasification furnace 1 to perform pyrolysis and gasification, the high-temperature synthesis gas generated by the pyrolysis and gasification is sent into the first group of dust removal heat exchangers 2 to perform dust removal and cooling, the synthesis gas after the dust removal and cooling is sent into the synthesis gas oxidation furnace 4 by using the high-temperature fan 3 to perform oxygen-rich combustion treatment, the gas generated by the combustion of the synthesis gas oxidation furnace 4 is subjected to dust removal and cooling treatment by the second group of dust removal heat exchangers 5 and then enters the primary purification system 6, the primary purification system performs preliminary treatment such as water washing, electrostatic dust removal and air cooling dust removal on the gas, after the preliminary treatment, the gas enters the secondary purification system 7 to perform filtration and activated carbon adsorption treatment, then the obtained carbon dioxide and nitrogen are sent into the carbon dioxide and nitrogen storage tank 9 by the Roots blower 8, the mixed gas of carbon dioxide and nitrogen in the carbon dioxide and nitrogen storage tank 9 is sent into the carbon dioxide and nitrogen separator 10, the carbon dioxide and nitrogen are separated by using the variable pressure adsorption separation, membrane separation or low-temperature deep cooling separation, the separated carbon dioxide is sent into the carbon dioxide storage tank 13, the carbon dioxide in the carbon dioxide storage tank 13 enters the green methanol catalytic synthesis reactor 11 to react with green hydrogen to synthesize green methanol, the obtained green methanol is stored in the green methanol storage tank 15, the separated nitrogen is sent into the nitrogen storage tank 14 and then into the green ammonia catalytic synthesis reactor 12 to synthesize green ammonia with the green hydrogen, the obtained green ammonia is stored in the green ammonia storage tank 16, and the heat generated when the first group of dust removal heat exchangers 2, the synthesis gas oxidation furnace 4 and the second group of dust removal heat exchangers 5 are running is recycled, and the recycled heat can be used for heat and power supply and cooling supply of the carbon dioxide and nitrogen separator 10.

[0029] Finally, it should be noted that: the above is only the preferred embodiment of the present application, and is not intended to limit the present application, although the present application has been described in detail with reference to the foregoing embodiments, for those skilled in the art, the technical solutions recorded in the foregoing embodiments can be modified, or some technical features can be replaced. Any modification, equivalent replacement, improvement, etc. made within the spirit and principles of the present application shall be included in the protection scope of the present application.

Claims

1. A system for producing green methanol and green ammonia by gasification and oxidation of biomass, comprising a biomass gasification furnace (1), characterized in that, The exhaust end of the biomass gasification furnace (1) is connected to the gas inlet end of the first group of dust removal heat exchangers (2) through a pipeline, the exhaust end of the first group of dust removal heat exchangers (2) is connected to the input end of the high-temperature fan (3) through a pipeline, the output end of the high-temperature fan (3) is connected to the synthetic gas oxidation furnace (4), the output end of the synthetic gas oxidation furnace (4) is connected to the second group of dust removal heat exchangers (5), the output end of the second group of dust removal heat exchangers (5) is sequentially connected to the primary purification system (6) and the secondary purification system (7) through a pipeline, the output end of the secondary purification system (7) is connected to the carbon dioxide and nitrogen gas storage tank (9) through the Roots blower (8), the output end of the carbon dioxide and nitrogen gas storage tank (9) is connected to the carbon dioxide and nitrogen gas separator (10), the output end of the carbon dioxide and nitrogen gas separator (10) is respectively connected to the carbon dioxide storage tank (13) and the nitrogen gas storage tank (14) through a pipeline, the output ends of the carbon dioxide storage tank (13) and the nitrogen gas storage tank (14) are respectively connected to the green methanol catalytic synthesis reactor (11) and the green ammonia catalytic synthesis reactor (12), the input ends of the green methanol catalytic synthesis reactor (11) and the green ammonia catalytic synthesis reactor (12) are connected to the green hydrogen storage tank through a pipeline, and the output ends of the green methanol catalytic synthesis reactor (11) and the green ammonia catalytic synthesis reactor (12) are respectively connected to the green methanol storage tank (15) and the green ammonia storage tank (16).

2. The system for producing green methanol and green ammonia by gasification and oxidation of biomass with air according to claim 1, characterized in that, The first group of dust removal heat exchangers (2) and the second group of dust removal heat exchangers (5) are both two-stage cyclone dust removal heat exchangers.

3. The system for producing green methanol and green ammonia by gasification and oxidation of biomass with air according to claim 1, characterized in that, The waste heat of the first group of dust removal heat exchangers (2), the second group of dust removal heat exchangers (5) and the synthetic gas oxidation furnace (4) is recovered for heat-electricity-cold supply and cooling of the carbon dioxide and nitrogen gas separator (10).

4. The system for producing green methanol and green ammonia by gasification and oxidation of biomass with air according to claim 1, characterized in that, The primary purification system (6) is spray water washing dust removal, electrostatic dust removal or air cooling dust removal, and the secondary purification system (7) is filter filtration and activated carbon adsorption.

5. The system for producing green methanol and green ammonia by gasification and oxidation of biomass with air according to claim 1, characterized in that, The carbon dioxide and nitrogen gas separator (10) is a pressure swing adsorption separator, a membrane separator or a low-temperature deep cooling separator.

6. The system for producing green methanol and green ammonia by gasification and oxidation of biomass with air according to claim 1, characterized in that, Green hydrogen is added to the green methanol catalytic synthesis reactor (11) to synthesize green methanol, and green hydrogen is added to the green ammonia catalytic synthesis reactor (12) to synthesize green ammonia. Green hydrogen is added to the green methanol catalytic synthesis reactor (11) to synthesize green methanol, and green hydrogen is added to the green ammonia catalytic synthesis reactor (12) to synthesize green ammonia.

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