Biomass comprehensive utilization method and system
By using additives with lattice oxygen storage and discharge properties in the process of hydrogen production of biomass gasification and converting CO2 into CO, the comprehensive utilization of biomass is achieved, and the problems of low hydrogen yield and unused CO2 in the prior art are solved, and efficient and low-carbon biomass resource utilization is achieved.
Patent Information
- Application Number
- CN202311643276.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2023-12-04
- Publication Date
- 2025-06-06
AI Technical Summary
The existing biomass gasification hydrogen production technology has problems such as difficult control of tar and low hydrogen yield. At the same time, the CO2 generated during the biomass conversion has not been effectively utilized.
During the biomass gasification process, the additives with lattice oxygen storage and discharge properties are used to gasify the biomass and produce hydrogen. At the same time, CO2 is converted into CO, and chemical products are produced through synthesis gas conversion units to achieve comprehensive utilization of biomass.
It realizes high added value utilization of biomass, improves hydrogen yield, and greatly reduces CO2 emissions, and improves the negative carbon and economicality of the biomass conversion process.
Smart Images
Figure CN120098675A_ABST
Abstract
Description
Technical Field
[0001] The present invention belongs to the technical field of biomass processing, and in particular relates to a method and system for producing high value-added products from biomass. Background Art
[0002] Biomass is green and renewable, and is increasingly gaining widespread attention and great attention from countries around the world. Promoting the resource utilization of abundant and green biomass materials, especially biomass hydrogen production, is an effective technical approach to achieving "dual carbon" and an important task for energy conservation, emission reduction and environmental protection in my country, which meets the current needs of environmental protection, energy conservation and low-carbon economy.
[0003] Biomass hydrogen production has the advantages of being green and low-carbon. Through thermochemical treatment, biomass is converted into hydrogen-rich combustible gas, and then pure hydrogen is obtained by separation. The main principle is: gasification hydrogen production refers to the process of converting hydrocarbons into hydrogen-containing combustible gas in a gasifying agent (such as air, water vapor, etc.). This technology has the problem of difficult control of tar. At present, biomass gasification hydrogen production requires the use of catalysts to accelerate medium and low temperature reactions. The main process is: biomass is heated and dried in a gasifier to evaporate water (100-200°C); as the temperature rises, the material begins to decompose and produce hydrocarbon gases. Subsequently, coke and pyrolysis products react with the introduced gasifying agent to undergo oxidation. As the temperature further increases (800-1000°C), the oxygen in the system is exhausted and the product begins to be reduced; the gasifying agents of biomass are mainly air, water vapor, oxygen, etc. When oxygen is used as a gasifying agent, the hydrogen production is high, but the energy consumption of preparing pure oxygen is high; when air is used as a gasifying agent, although the cost is low, there is a large amount of nitrogen that is difficult to separate. At present, thermochemical hydrogen production from biomass has partially achieved a certain scale of production, but the hydrogen yield is generally not high.
[0004] From CO 2 From a different perspective, biomass always produces CO during its conversion and utilization. 2 According to current standards, this part of CO is generally not considered 2 However, if this part of CO 2 If converted and utilized, the carbon negativity and economic efficiency of the biomass conversion process will be further improved. Summary of the invention
[0005] In view of the shortcomings of the prior art, the present invention provides a method and system for comprehensive utilization of biomass. The present invention makes full use of the resource properties of biomass, gasifies biomass under the action of an additive with lattice oxygen storage and release properties; at the same time, uses a hydrogen production unit to provide a hydrogen source to convert CO 2 It is converted into CO and chemical products are produced through the synthesis gas conversion unit, realizing the comprehensive utilization of biomass and significantly reducing CO 2 emission.
[0006] The first aspect of the present invention provides a method for comprehensive utilization of biomass, comprising the following steps:
[0007] (1) The biomass raw material enters the biomass gasification unit and reacts in the presence of an auxiliary agent, thereby obtaining a first gas phase stream and a first solid phase stream;
[0008] (2) The first gas phase stream obtained in step (1) is contacted with calcium oxide in a reaction unit for reaction, and a second gas phase stream and a second solid phase stream are obtained after the reaction;
[0009] (3) water vapor enters the hydrogen production unit and reacts in the presence of the first solid phase stream obtained in step (1), thereby obtaining a third gas phase stream and a third solid phase stream;
[0010] (4) The third gas phase stream obtained in step (3) is condensed and then enters a heat conversion unit with the second solid phase stream obtained in step (2) to react, thereby obtaining a fourth gas phase stream and a fourth solid phase stream.
[0011] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific implementation, the operating conditions of the biomass gasification unit in step (1) are as follows: the reaction temperature is 400-1000°C, preferably 500-700°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa; the biomass gasification unit can adopt a moving bed reactor.
[0012] Furthermore, in the above-mentioned method for comprehensive utilization of biomass, as a specific implementation method, the biomass raw material described in step (1) can be derived from any material containing lignocellulose, and can be one or more of corn stalks, rice husks, wheat straw, and wood chips; the biomass raw material is generally first dried and dehydrated, and the drying and dehydration treatment is preferably carried out by microwave drying, the microwave frequency is generally 2400±500MHZ, the drying time is 5-20min, and the moisture content of the biomass after dehydration is usually controlled to be 5-20wt%.
[0013] Furthermore, in the above-mentioned method for comprehensive utilization of biomass, as a specific implementation, the second gas phase stream obtained by the reaction unit in step (2) can enter the synthesis gas conversion unit to participate in the reaction.
[0014] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific implementation, the operating conditions of the hydrogen production unit in step (3) are as follows: the reaction temperature is 500-1000°C, preferably 600-900°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa.
[0015] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific embodiment, the first gas phase stream includes carbon monoxide, carbon dioxide and hydrogen, and further the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase stream can be controlled to be 1-10:0.1-5:99-85, preferably 3-5:2-3:95-90.
[0016] Furthermore, in the above-mentioned method for comprehensive utilization of biomass, as a specific embodiment, the auxiliary agent in step (1) is a composite oxide containing Fe, Ti, and Mn elements. Based on the weight of the composite oxide, the weight content of iron oxide in the composite oxide is 20%-85%, preferably 50-75%; the weight content of titanium oxide is 10-65%, preferably 20-40%; the weight content of manganese oxide is 1-15%, preferably 5-10%.
[0017] Furthermore, in the above-mentioned method for comprehensive utilization of biomass, as a specific implementation, the mass ratio of the biomass raw material to the auxiliary agent in step (1) is 1:(1-20), preferably 1:(2-10).
[0018] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific embodiment, the third solid phase stream obtained in step (3) enters the oxidation unit to contact with the oxygen-containing atmosphere for reaction, and the solid phase material obtained after the reaction can be recycled to the biomass gasification unit for use. The operating conditions of the oxidation unit are as follows: the reaction temperature is 500-1200°C, preferably 700-1000°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa. The oxygen-containing atmosphere can be oxygen, air, etc.
[0019] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific embodiment, the reaction conditions of the heat conversion unit in step (4) are as follows: the reaction temperature is 500-1200°C, preferably 600-800°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa. The heat conversion reactor used in the heat conversion unit can be one or more of a fixed bed reactor, a moving bed reactor, a fluidized bed reactor, and an ebullient bed reactor.
[0020] Furthermore, in the above-mentioned biomass comprehensive utilization method, as a specific embodiment, the fourth gas phase stream obtained in step (4) can enter the synthesis gas conversion unit for reaction. The reaction conditions of the synthesis gas conversion unit are as follows: the reaction temperature is 200-500°C, preferably 220-400°C; the reaction pressure is 0.1-10Mpa, preferably 0.5-6Mpa.
[0021] Furthermore, in the above-mentioned method for comprehensive utilization of biomass, as a specific embodiment, the fourth solid phase stream obtained in step (4) is recycled back to the reaction unit in step (2) to contact and react with the first gas phase stream.
[0022] In addition, the present invention also provides a biomass comprehensive utilization system, which includes a biomass gasification unit, a reaction unit, a hydrogen production unit, and a thermal conversion unit;
[0023] A biomass gasification unit, which is used to receive biomass and react it in the presence of an auxiliary agent to obtain a first gas phase stream and a first solid phase stream;
[0024] A reaction unit, which is used to receive calcium oxide and a first gaseous material stream obtained from a biomass gasification unit, and the first gaseous material stream is contacted with the calcium oxide to react to obtain a second gaseous material stream and a second solid-phase material stream;
[0025] A hydrogen production unit, which is used to receive water vapor and a first solid-phase stream obtained from a biomass gasification unit, and obtain a third gas-phase stream and a third solid-phase stream after reaction;
[0026] The heat conversion unit is used to receive the gaseous materials after condensation of the second solid-phase material flow from the reaction unit and the third gas-phase material flow from the hydrogen production unit, and obtain the fourth gas-phase material flow and the fourth solid-phase material flow after reaction.
[0027] Furthermore, in the above-mentioned biomass comprehensive utilization system, as a specific embodiment, the comprehensive utilization system includes an oxidation unit, which is used to receive the third solid phase feed stream and the oxygen-containing atmosphere from the hydrogen production unit, and the third solid phase feed stream contacts with the oxygen-containing atmosphere to react, and the solid phase material obtained after the reaction can be recycled to the biomass gasification unit for use.
[0028] Furthermore, in the above-mentioned biomass comprehensive utilization system, as a specific embodiment, the comprehensive utilization system includes a drying unit, which is used to receive and dry and dehydrate the biomass; the drying unit adopts microwave drying, the microwave drying condition is 2400±500MHZ, the drying time is 5-20min, and the water content of the biomass raw material after dehydration is 5-20wt%. The water removed by drying can be used for hydrogen production reaction.
[0029] Furthermore, in the above-mentioned biomass comprehensive utilization system, as a specific embodiment, the comprehensive utilization system includes a condenser, which is used to condense the third gas phase stream from the hydrogen production unit, and the water obtained by condensation enters the hydrogen production unit after passing through a mixer. The gas phase material after condensation of the third gas phase stream can also enter the synthesis gas conversion unit for reaction.
[0030] Furthermore, in the above-mentioned biomass comprehensive utilization system, as a specific embodiment, the comprehensive utilization system includes a synthesis gas conversion unit, which is used to receive the fourth gas phase feed stream from the thermal conversion unit, and the fourth gas phase feed stream mainly includes hydrogen and carbon monoxide. Hydrogen and carbon monoxide undergo synthesis gas conversion reaction under different proportions and conditions to generate reaction products such as light olefins, methanol, or methane.
[0031] Compared with the prior art, the main beneficial effects of the technical solution provided by the present invention are mainly reflected in the following aspects:
[0032] 1. The method of the present invention provides a high value-added utilization approach for biomass, organically combining biomass gasification, hydrogen production and other reactions into a whole.
[0033] 2. In the method for comprehensive utilization of biomass provided by the present invention, the auxiliary agent in step (1) can be recycled among the biomass gasification unit, the hydrogen production unit and the oxidation unit. First, it can promote the biomass gasification reaction in the biomass gasification unit. The auxiliary agent will lose lattice oxygen and convert into a reduced state during the gasification reaction. In the hydrogen production unit, it will greatly promote the water vapor hydrogen production reaction. The auxiliary agent after the reaction in the hydrogen production unit enters the oxidation unit for further oxidation reaction and then circulates back to the gasification unit for repeated use.
[0034] 3. In the method for comprehensive utilization of biomass provided by the present invention, the first gas phase stream and calcium oxide enter the reaction unit for contact and reaction. The calcium oxide can react with the carbon dioxide in the first gas phase stream to separate and purify the first gas phase stream. The second gas phase stream obtained after treatment mainly consists of carbon monoxide and hydrogen, which can be converted into synthesis gas for chemical utilization.
[0035] 4. In the method for comprehensive utilization of biomass provided by the present invention, the second solid-phase feed stream contacts the condensed gaseous material of the third gas-phase feed stream to carry out a thermal conversion reaction. The introduction of the third gas-phase feed stream can significantly promote the thermal conversion reaction and improve the conversion efficiency, and also reduce the temperature of the thermal conversion reaction. At the same time, the composition of the fourth gas-phase feed stream can also be regulated to reduce the proportion of carbon dioxide in the fourth gas-phase feed stream and increase the proportion of carbon monoxide. BRIEF DESCRIPTION OF THE DRAWINGS
[0036] Figure 1 It is a schematic diagram of the biomass comprehensive utilization method and system provided by the present invention.
[0037] 1. Dehydration unit; 2. Biomass gasification unit; 3. Reaction unit; 4. Hydrogen production unit; 5. Mixer; 6. Condenser; 7. Thermal conversion unit; 8. Synthesis gas conversion unit; 9. Oxidation unit; 11. Biomass feedstock; 21. 1st gas stream; 22. 1st solid stream; 31. 2nd gas stream; 32. 2nd solid stream; 41. 3rd gas stream; 42. 3rd solid stream; 51. Water; 71. 4th gas stream; 72. 4th solid stream; 81. Reaction product; 91. 5th gas stream; 92. 5th solid stream; 93. Oxygen-containing atmosphere. DETAILED DESCRIPTION
[0038] The biomass comprehensive utilization method and system provided by the present invention will be further described below in conjunction with the accompanying drawings and specific implementation examples.
[0039] Unless explicitly stated otherwise, throughout the specification and claims, the term “comprise” or variations such as “include” or “comprising”, etc., will be understood to include the stated elements or components but not to exclude other elements or components.
[0040] In this document, for the convenience of description, spatial relative terms such as "below", "below", "down", "above", "above", "upper", etc. may be used to describe the relationship between one element or feature and another element or feature in the accompanying drawings. It should be understood that the spatial relative terms are intended to include different orientations of the object in use or operation in addition to the orientation depicted in the figure. For example, if the object in the figure is turned over, the element described as being "below" or "below" other elements or features will be oriented "above" the element or feature. Therefore, the exemplary term "below" can include both below and above. Objects may also have other orientations (rotated 90 degrees or other orientations) and the spatial relative terms used in this document should be interpreted accordingly.
[0041] In this document, the terms "first", "second", etc. are used to distinguish two different elements or parts, and are not used to limit a specific position or relative relationship. In other words, in some embodiments, the terms "first", "second", etc. can also be interchangeable.
[0042]
[0043] In this document, all numerical values for parameters (eg, amounts or conditions) are to be understood as being modified in all instances by the term "about", whether or not "about" actually appears before the numerical value.
[0043] The specific process flow of the biomass comprehensive utilization method provided by the present invention is as follows: the biomass raw material 11 first enters the dehydration unit 1 for drying and dehydration treatment, and the biomass raw material after drying and dehydration treatment enters the biomass gasification unit 2, reacts in the presence of an auxiliary agent, and obtains a first gas phase stream 21 and a first solid phase stream 22 after the reaction; the obtained first gas phase stream 21 and calcium oxide enter the reaction unit 3 to contact each other and react, and obtain a second gas phase stream 31 and a second solid phase stream 32 after the reaction; water 51 and the water after the biomass is dried and dehydrated are mixed in the mixer 5 and enter the hydrogen production unit 4, and contact and react with the first solid phase stream 22 obtained in step (1), and obtain a third gas phase stream after the reaction. The obtained third solid-phase stream 42 enters the oxidation unit 9, and is subjected to oxidation regeneration reaction in the presence of an oxygen-containing atmosphere 93, and after the reaction, the fifth gas-phase stream 91 and the fifth solid-phase stream 92 are obtained, and the fifth solid-phase stream 92 enters the biomass gasification unit 2 to participate in the reaction; the obtained third gas-phase stream 41 enters the condenser 6, and the part of the gas-phase material after condensation enters the thermal conversion unit 7 with the second solid-phase stream 32 to react, and after the reaction, the fourth gas-phase stream 71 and the fourth solid-phase stream 72 are obtained, wherein the part of the gas-phase material after condensation of the fourth gas-phase stream 71 and the third gas-phase stream 41 enters the synthesis gas conversion unit 8 to react, and after the reaction, the reaction product 81 is obtained. The obtained fourth solid-phase stream 72 is circulated back to the reaction unit 3 to contact with the first gas-phase stream 21 for reaction.
[0044] Example 1
[0045] (1) Forest biomass as raw material (24 kg / h) enters the microwave drying device and is dehydrated under the conditions of 2400 MHZ and drying time of 150 min. The moisture content of the treated biomass raw material is 7.0 wt%.
[0046] (2) The oxidized additives obtained from the oxidation unit (solid circulation rate of 120 kg / h, 61.2 wt% iron oxide; 31.9 wt% titanium oxide; 6.9 wt% manganese oxide) are co-flowed with the microwave-dried biomass into the gasification unit, and the gasification reaction is carried out at 700°C and 0.6 MPa to obtain high-temperature fuel gas (CO 2 10.02wt%, CO 81.31wt%, H 2 4.87wt%,H 2 O3.80wt%); the auxiliary agent after the reaction enters the hydrogen production unit.
[0047] (3) Contains CO 2 The high-temperature fuel gas enters the reaction unit, and the CO 2 It reacts with CaO in countercurrent flow to form CaCO 3 , CO removal 2The decarbonized gas (CO 94.35wt%, H 2 5.65wt%), and at the same time, the CaCO generated by the reaction 3 Enter the thermal conversion unit for reaction.
[0048] (4) Fresh water (5.8 kg / h) is mixed with water obtained from a microwave drying device and condensed water from a hydrogen production reactor, and then countercurrently contacts with a reduced additive in the hydrogen production unit, where a steam reforming hydrogen production reaction occurs at 800°C and 0.6 MPa to generate a mixture of hydrogen and water vapor. The condensed water obtained after condensation is circulated to the mixer; a portion of the hydrogen (2.1 kg / h) without condensed water enters the thermal conversion unit, and the other portion of the hydrogen is used to adjust the hydrogen-carbon ratio of the synthesis gas. The additive after the reaction is discharged downward from the bottom of the hydrogen production unit and enters the oxidation unit.
[0049] (5) The auxiliary agent discharged from the bottom of the hydrogen production reactor enters the oxidation unit under the fluidization action of the oxygen-containing gas (oxygen content is 3%), undergoes oxidation reaction with the oxygen-containing gas at 850°C and 0.6MPa to generate an oxidized auxiliary agent, which is then separated from the gas and solid by a cyclone separator. The resulting solid enters the gasification unit, and the resulting gas is discharged as regeneration flue gas.
[0050] (6) CaCO obtained from the reaction unit 3 The solid enters the thermal conversion unit, and the hydrogen from the hydrogen production unit enters from the bottom of the reactor as fluidizing air. The reaction occurs at 650°C and 0.6 MPa, and the gases generated are CO and H 2 ; The solid CaO discharged from the bottom of the reactor is circulated into the reaction unit.
[0051] (7) CO and H obtained from the thermal conversion unit 2 The mixture, together with the hydrogen obtained from the hydrogen production unit, is fed into the synthesis gas conversion unit after adjusting the hydrogen-carbon ratio of the synthesis gas. 2 / CO=2.2, the product is C2~C4 low carbon olefins; there is no CO in the whole process. 2 emission.
[0052] Example 2
[0053] The process flow of Example 2 is the same as that of Example 1, except that the composition of the additive is 72.4 wt% iron oxide; 22.5 wt% titanium oxide; 5.1 wt% manganese oxide; in the synthesis gas conversion unit, at 230°C, 5.2 MPa, H 2 The product obtained by the reaction was methanol.
[0054] Example 3
[0055] The process flow of Example 3 is the same as that of Example 1, except that the composition of the additive is 55.2 wt% iron oxide; 38.6 wt% titanium oxide; 6.2 wt% manganese oxide; in the synthesis gas conversion unit, at 310°C, 3.5 MPa, H 2 The reaction was carried out at / CO=3.05 to obtain methane as the product.
[0056] Comparative Example 1
[0057] The difference between Comparative Example 1 and Example 1 is that no reaction unit and thermal conversion unit are set. Under the same operating parameters, CO 2 The emission is 2.8kg / h.
Claims
1. A method for comprehensive utilization of biomass, comprising the following steps: (1) The biomass raw material enters the biomass gasification unit and reacts in the presence of an auxiliary agent, thereby obtaining a first gas phase stream and a first solid phase stream; (2) The first gas phase stream obtained in step (1) is contacted with calcium oxide in a reaction unit for reaction, and a second gas phase stream and a second solid phase stream are obtained after the reaction; (3) water vapor enters the hydrogen production unit and reacts in the presence of the first solid phase stream obtained in step (1), thereby obtaining a third gas phase stream and a third solid phase stream; (4) The third gas phase stream obtained in step (3) is condensed and then enters a heat conversion unit with the second solid phase stream obtained in step (2) to react, thereby obtaining a fourth gas phase stream and a fourth solid phase stream.
2. The method for comprehensive utilization of biomass according to claim 1, Features: The operating conditions of the biomass gasification unit in step (1) are as follows: the reaction temperature is 400-1000°C, preferably 500-700°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa.
3. The method for comprehensive utilization of biomass according to claim 1, Features: The biomass raw material in step (1) is derived from any material containing lignocellulose, and is selected from one or more of corn stalks, rice husks, wheat straw, and wood chips.
4. The method for comprehensive utilization of biomass according to claim 1, Features: The biomass raw material is dried and dehydrated, and the moisture content of the biomass after the dehydration treatment is 5-20wt%.
5. The method for comprehensive utilization of biomass according to claim 1, Features: The second gas phase stream obtained in the reaction unit in step (2) enters the synthesis gas conversion unit to participate in the reaction.
6. The method for comprehensive utilization of biomass according to claim 1, Features: The operating conditions of the hydrogen production unit in step (3) are as follows: the reaction temperature is 500-1000°C, preferably 600-900°C; the reaction pressure is 0.1-2Mpa, preferably 0.5-1Mpa.
7. The method for comprehensive utilization of biomass according to claim 1, Features: The first gas phase feed stream includes carbon monoxide, carbon dioxide and hydrogen. Further, the molar ratio of carbon monoxide, carbon dioxide and hydrogen in the first gas phase feed stream is 1-10:0.1-5:99-85, preferably 3-5:2-3:95-90.
8. The method for comprehensive utilization of biomass according to claim 1, Features: The auxiliary agent in step (1) is a composite oxide containing Fe, Ti and Mn elements. Based on the weight of the composite oxide, the weight content of iron oxide in the composite oxide is 20%-85%, preferably 50-75%; the weight content of titanium oxide is 10-65%, preferably 20-40%; and the weight content of manganese oxide is 1-15%, preferably 5-10%.
9. The method for comprehensive utilization of biomass according to claim 1, Features: The mass ratio of the biomass raw material to the auxiliary agent in step (1) is 1:(1-20), preferably 1:(2-10).
10. The method for comprehensive utilization of biomass according to claim 1, Features: The third solid phase material flow obtained in step (3) enters the oxidation unit to contact with the oxygen-containing atmosphere for reaction, and the solid phase material obtained after the reaction is recycled to the biomass gasification unit for use.
11. The method for comprehensive utilization of biomass according to claim 10, Features: The operating conditions of the oxidation unit are as follows: the reaction temperature is 500-1200° C., preferably 700-1000° C.; the reaction pressure is 0.1-2 MPa, preferably 0.5-1 MPa.
12. The method for comprehensive utilization of biomass according to claim 1, Features: The reaction conditions of the heat conversion unit in step (4) are as follows: the reaction temperature is 500-1200° C., preferably 600-800° C.; the reaction pressure is 0.1-2 MPa, preferably 0.5-1 MPa.
13. The method for comprehensive utilization of biomass according to claim 1, Features: The fourth gas phase stream obtained in step (4) enters the synthesis gas conversion unit for reaction; the reaction conditions of the synthesis gas conversion unit are as follows: the reaction temperature is 200-500°C, preferably 220-400°C; the reaction pressure is 0.1-10Mpa, preferably 0.5-6Mpa.
14. The method for comprehensive utilization of biomass according to claim 1, Features: The fourth solid phase stream obtained in step (4) is recycled back to the reaction unit in step (2) to contact with the first gas phase stream for reaction.
15. A biomass comprehensive utilization system, comprising a biomass gasification unit, a reaction unit, a hydrogen production unit, and a thermal conversion unit; A biomass gasification unit, which is used to receive biomass and react it in the presence of an auxiliary agent to obtain a first gas phase stream and a first solid phase stream; A reaction unit, which is used to receive a first gas-phase material flow and calcium oxide obtained from a biomass gasification unit, and obtain a second gas-phase material flow and a second solid-phase material flow after the first gas-phase material flow contacts and reacts with the calcium oxide; A hydrogen production unit, which is used to receive water vapor and a first solid-phase stream obtained from a biomass gasification unit, and obtain a third gas-phase stream and a third solid-phase stream after reaction; The heat conversion unit is used to receive the gaseous materials after condensation of the second solid-phase material flow from the reaction unit and the third gas-phase material flow from the hydrogen production unit, and obtain the fourth gas-phase material flow and the fourth solid-phase material flow after reaction.
16. The biomass comprehensive utilization system according to claim 15, Features: The comprehensive utilization system includes an oxidation unit, which is used to receive the third solid phase stream and the oxygen-containing atmosphere from the hydrogen production unit. The third solid phase stream contacts the oxygen-containing atmosphere for reaction, and the solid phase material obtained after the reaction is recycled to the biomass gasification unit for use.
17. The biomass comprehensive utilization system according to claim 15, Features: The comprehensive utilization system comprises a drying unit, which is used for receiving and performing drying and dehydration treatment on biomass.
18. The biomass comprehensive utilization system according to claim 15, Features: The comprehensive utilization system includes a synthesis gas conversion unit, which is used to receive the fourth gas phase feed stream from the thermal conversion unit. The fourth gas phase feed stream mainly includes hydrogen and carbon monoxide. Hydrogen and carbon monoxide undergo synthesis gas conversion reaction at different proportions to produce light olefins, methanol or methane.