Anaerobic fermentation mediated biomass multi-source atmosphere gasification hydrogen production system and operation method thereof

Abstract

The invention belongs to the technical field of hydrogen preparation, and provides an anaerobic fermentation mediated biomass multi-source atmosphere gasification hydrogen production system and an operation method thereof, and the system comprises a complete mixing type continuous anaerobic reaction tank, a biogas compression temporary storage tank, a separation dryer, a water vapor transmitter, a spiral feeder, a gasification reaction bed, a cyclone separator and a hydrogen purification tower. Marsh gas obtained by anaerobic fermentation in the full-mixing type continuous anaerobic reaction tank is conveyed to the front of a gas inlet valve of the gasification reaction bed through a marsh gas compression temporary storage tank; water vapor generated by the water vapor transmitter is premixed with biogas and then passes through the gasification reaction bed; biogas residues generated by the full-mixing type continuous anaerobic reaction tank are conveyed into the spiral feeder through the separation dryer; biogas residues in the spiral feeder are conveyed into the gasification reaction bed; the water vapor, the biogas and the biogas residues are subjected to a hydrogen production reaction in the gasification reaction bed to obtain a gasification product; and conveying the gasified product to a hydrogen purification tower through a cyclone separator to obtain hydrogen, thereby completing the operation.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen production, in particular to an anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system and a running method thereof. BACKGROUND

[0002] Hydrogen energy is a high-efficiency, clean and carbon-free energy carrier. However, 96% of the hydrogen produced globally is still dependent on fossil fuels, and the production of 1 ton of hydrogen is accompanied by the emission of 9-12 tons of carbon dioxide, which has a significant impact on the environment. Therefore, the development of green hydrogen production technology has become a key to global energy transformation. Among the many renewable energy hydrogen production methods, biomass hydrogen production is of great concern due to the abundance of raw materials and the fact that the process is not limited by geography and weather. In this context, it has significant strategic significance to convert biomass into high-value green hydrogen.

[0003] Biomass steam gasification technology refers to a hydrogen production gasification technology that uses steam instead of part of the air / oxygen medium to strengthen hydrogen production. This technology can improve hydrogen selectivity by strengthening chemical processes such as methane wet reforming (CH4+H2O→CO+3H2) and water gas reaction (C+H2O→CO+H2), and the hydrogen content in the syngas can reach more than 50%. In addition, the steam gasification technology has high adaptability to the water content of the raw materials (usually up to 30%-50%), which can effectively reduce the energy consumption of the pretreatment of high-moisture biomass. However, this technology still has the problem of steam-energy dynamic balance: excessive steam input will cause heat dilution in the gasification zone, which is not conducive to the progress of endothermic reactions, and the sensible heat loss in the steam generation process will significantly reduce the energy efficiency of the process; when the steam supply is insufficient, the hydrogen production strengthening effect is limited, and it is difficult to achieve a substantial breakthrough in hydrogen yield. Therefore, the hydrogen production strengthening of the single steam medium has a theoretical limit.

[0004] Therefore, it is an urgent problem to provide an efficient hydrogen production method. SUMMARY

[0005] The present application aims to overcome the defects in the prior art and provide an anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system and a running method thereof.

[0006] In order to achieve the above-mentioned application purposes, the present application provides the following technical solutions: The present application provides an anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system, which comprises a full-mixing continuous anaerobic reaction tank, a biogas compression temporary storage tank, a separation dryer, a steam sender, a screw feeder, a gasification reaction bed, a cyclone separator and a hydrogen purification column.

[0007] As a preferred, the full-mixing continuous anaerobic reaction tank is connected with the biogas compression temporary storage tank through a gas production and exhaust port, and the full-mixing continuous anaerobic reaction tank is connected with the separation dryer through a residue discharge port.

[0008] As preferred, the separation dryer is connected with the screw feeder; the gasification reaction bed is communicated with the biogas compression temporary storage tank, the water vapor sender and the screw feeder.

[0009] As preferred, the gasification reaction bed is connected with the hydrogen gas purification tower through the cyclone separator.

[0010] The application also provides a running method of the anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system, containing the following steps: (1) the biogas obtained by anaerobic fermentation in the full-mixing type continuous anaerobic reaction tank is transported to the front of the gasification reaction bed gas inlet valve through the biogas compression temporary storage tank; the water vapor generated by the water vapor sender is premixed with the biogas and then transported through the gasification reaction bed; (2) the biogas residue generated by the full-mixing type continuous anaerobic reaction tank is transported through the separation dryer and then transported into the screw feeder; the biogas residue in the screw feeder is transported into the gasification reaction bed; (3) the water vapor, the biogas and the biogas residue are subjected to hydrogen production reaction in the gasification reaction bed to obtain gasification products; the gasification products are transported to the hydrogen gas purification tower through the cyclone separator to obtain hydrogen gas, and the running is completed.

[0011] As preferred, the total solid concentration of the reaction raw material in step (1) is 4-6%.

[0012] As preferred, the reaction temperature of the anaerobic fermentation in step (1) is 35-55℃, and the hydraulic retention time is 10-30 days.

[0013] As preferred, the mass ratio of the water vapor and the biogas residue in step (3) is ≤8.

[0014] As preferred, the carrier gas flow rate in step (3) is 100-300 mL / min.

[0015] As preferred, the gasification temperature in step (3) is 700-900℃, and the time is 10-60 min.

[0016] The application provides an anaerobic fermentation mediated biomass multi-source atmosphere gasification hydrogen production system, which comprises a full-mixing type continuous anaerobic reaction tank, a biogas compression temporary storage tank, a separation dryer, a water vapor sender, a screw feeder, a gasification reaction bed, a cyclone separator and a hydrogen purification tower. The full-mixing type continuous anaerobic reaction tank is connected with the biogas compression temporary storage tank through a gas production and exhaust port, and is connected with the separation dryer through a residue discharge port. The separation dryer is connected with the screw feeder; the gasification reaction bed is in communication with the biogas compression temporary storage tank, the water vapor sender and the screw feeder. The gasification reaction bed is connected with the hydrogen purification tower through the cyclone separator. The biogas produced by anaerobic fermentation in the full-mixing type continuous anaerobic reaction tank is transported to the front of a gas inlet valve of the gasification reaction bed through the biogas compression temporary storage tank; the water vapor generated by the water vapor sender is premixed with the biogas and then passes through the gasification reaction bed; the biogas residue produced by the full-mixing type continuous anaerobic reaction tank is transported to the screw feeder through the separation dryer; the biogas residue in the screw feeder is transported into the gasification reaction bed; the water vapor, the biogas and the biogas residue are subjected to a hydrogen production reaction in the gasification reaction bed to obtain a gasification product; the gasification product is transported to the hydrogen purification tower through the cyclone separator to obtain hydrogen, and the operation is completed.

[0017] In the application, the anaerobic fermentation can convert part of the organic components into biogas (mainly carbon dioxide and methane) through the action of microorganisms, and the refractory components are left in the solid to form biogas residue; the CO2 in the biogas can be used as a water vapor gasification common atmosphere to reduce the cost of the gasification agent and achieve CO2 capture, while the CH4 in the biogas can provide sufficient carbon and hydrogen source supply for the reforming reaction of the gasification process to realize the secondary release of hydrogen elements. Therefore, the multi-source atmosphere system constructed by the CO2 / CH4 components in the biogas and water vapor has significant advantages in hydrogen production by gasification. On the other hand, compared with the original biomass, the fermented biogas residue still contains a large amount of organic components (volatile content > 60%), and shows the evolution characteristics of reduced cellulose / hemicellulose content and relatively enriched lignin. Among the three components, hemicellulose is more prone to form tar, and lignin forms aromatic hydrocarbons and hydrogen, so the generation of tar is inhibited and the generation of hydrogen is promoted from the raw material end. In addition, compared with the strict limitation (< 20%) of the water content of the raw material in the traditional gasification, the water vapor gasification has higher adaptability (30%~50%) to the water content of the raw material, effectively avoiding the high energy consumption demand of the traditional pyrolysis gasification for drying the raw material; at the same time, part of the endogenous water can act as a gasification agent, and its self-evaporation effect accelerates the evolution of the semi-coke pore, and the secondary reaction of water molecules with intermediate products effectively improves the hydrogen production performance.

[0018] In the application, the anaerobic fermentation is used as a "mediation", and the biogas product thereof is introduced into the water vapor gasification system, which can effectively strengthen the hydrogen production path and realize the in-situ application and efficient hydrogen production of biogas; and the high-moisture biogas residue by-product as a gasification raw material shows significant technical adaptability with the water vapor gasification technology, and through the control of the anaerobic fermentation degree and the synergistic adjustment of the biogas and water vapor atmosphere, the efficient hydrogen production of biomass is realized. BRIEF DESCRIPTION OF DRAWINGS

[0019] Figure 1 Flow chart of the anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system of the present application; Figure 2 Figure for biogas production under different hydraulic retention times in Example 1; Figure 3 Figure for hydrogen production and proportion comparison of Example 2 and Example 3; Figure 4 Figure for hydrogen production and proportion comparison of Example 4 and Example 5; Figure 5 Figure for hydrogen production and proportion comparison of Example 5 and Example 2; Figure 6 Figure for hydrogen production and proportion of Example 4, Example 5, Example 6, Example 7 and Example 8. DETAILED DESCRIPTION

[0020] The present application provides an anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system, comprising a full-mixing continuous anaerobic reaction tank, a biogas compression temporary storage tank, a separation dryer, a water vapor sender, a screw feeder, a gasification reaction bed, a cyclone separator and a hydrogen purification column.

[0021] In the present application, the full-mixing continuous anaerobic reaction tank is connected with the biogas compression temporary storage tank through a gas production and exhaust port, and the full-mixing continuous anaerobic reaction tank is connected with the separation dryer through a residue discharge port.

[0022] In the present application, the separation dryer is connected with the screw feeder, and the gasification reaction bed is in communication with the biogas compression temporary storage tank, the water vapor sender and the screw feeder.

[0023] In the present application, the gasification reaction bed is connected with the hydrogen purification column through the cyclone separator.

[0024] The present application also provides a running method of the anaerobic fermentation mediated biomass multi-source gas atmosphere gasification hydrogen production system, characterized by comprising the following steps: (1) The biogas obtained by anaerobic fermentation in the full-mixing continuous anaerobic reaction tank is transported to the front of the gasification reaction bed inlet valve through the biogas compression temporary storage tank; the water vapor generated by the water vapor sender is premixed with the biogas and then passes through the gasification reaction bed; (2) The biogas residue generated by the full-mixing continuous anaerobic reaction tank is transported to the screw feeder through the separation dryer; the biogas residue in the screw feeder is transported into the gasification reaction bed; (3) The water vapor, biogas and biogas residue in the gasification reaction bed perform hydrogen production reaction to obtain gasification products; the gasification products are transported to the hydrogen purification column through the cyclone separator to obtain hydrogen, and the running is completed.

[0025] In the present application, the biomass raw material used in anaerobic fermentation comprises one or more of kitchen sludge, kitchen waste, straw, microalgae, rice hulls, potato residue and sugarcane residue.

[0026] In the present application, the total solid concentration of the reaction raw material in step (1) is preferably 4-6%, further preferably 4.5-5.5%, and more preferably 4.8-5.2%.

[0027] In the present application, the reaction temperature in step (1) is preferably 35-55℃, further preferably 40-50℃, and more preferably 43-47℃; the hydraulic retention time is preferably 10-30 days, further preferably 15-25 days, and more preferably 18-23 days.

[0028] In the present application, the biogas produced in step (2) is transported to a sewage treatment plant for centralized treatment after preliminary purification; the ash produced after gasification is collected for land improvement.

[0029] In the present application, the function of the cyclone separator in step (3) is to remove impurities such as tar, and the gas enters the hydrogen purification tower for purification, and the hydrogen after separation and purification is stored in the hydrogen storage tank.

[0030] In the present application, the mass ratio of water vapor to biogas residue in the hydrogen production reaction in step (3) is preferably ≤8, further preferably 7, 6, 5, 4, 3, 2, or 1.

[0031] In the present application, the carrier gas flow rate in the hydrogen production reaction in step (3) is preferably 100-300 mL / min, further preferably 150-250 mL / min, and more preferably 180-220 mL / min.

[0032] In the present application, the gasification temperature in the hydrogen production reaction in step (3) is preferably 700-900℃, further preferably 750-850℃, and more preferably 780-820℃; the time is preferably 10-60 min, further preferably 20-50 min, and more preferably 30-40 min.

[0033] The present application takes biomass organic solid waste as raw material, and converts the fermentation biogas residue into hydrogen through anaerobic fermentation mediation to construct a multi-source gas atmosphere of biogas and water vapor. The specific advantages are as follows: first, the moderate fermentation of biomass is used to obtain biogas products, which can effectively shorten the fermentation period, and at the same time, the dense structure of biomass is moderately depolymerized and the generation of tar is inhibited from the source; second, the biogas and water vapor generated by fermentation are used as gasification agents, which can increase the water content of the gasification raw material to reduce the drying energy consumption, and at the same time, the hydrogen production process is strengthened and the in-situ application of biogas is realized. Finally, through the synergistic regulation of the fermentation degree and the gasification parameters, the biomass conversion efficiency and the hydrogen production rate can be significantly improved, and the hydrogen production rate can reach 319.61 mL / g.

[0034] The flow chart of the anaerobic fermentation mediation biomass multi-source gas atmosphere gasification hydrogen production system of the present application is shown in Figure 1

[0035] The technical solutions provided by the present application will be described in detail below in conjunction with examples, but they should not be understood as limiting the scope of protection of the present application.

[0036] Example 1

[0037] The hydrogen production system is built: the full-mixing type continuous anaerobic reaction tank is connected with the biogas compression temporary storage tank through the gas discharge port, the full-mixing type continuous anaerobic reaction tank is connected with the separation dryer through the residue discharge port, the separation dryer is connected with the screw feeder, the gasification reaction bed is in communication with the biogas compression temporary storage tank, the water vapor sender and the screw feeder, and the gasification reaction bed is connected with the hydrogen purification tower through the cyclone separator.

[0038] The biomass raw material is kitchen biogas residue. Before the formal experiment starts, the total solid concentration (TS) of the initial running device is set to 5%, and then the anaerobic reactor is domesticated with the parameters of hydraulic retention time (HRT) of 60d, organic loading rate (OLR) of 0.93gTS / L / d and TS of 5%. When the gas production performance of the reactor is stable, the HRT is reduced, and 30, 20 and 10 days are set as experimental groups respectively, and the running time of each group is 20d, and the temperature is controlled at 35℃. The unloading and feeding are carried out at the same time every day, and the biogas and biogas residue are collected for subsequent gasification experiment.

[0039] The biogas production under different hydraulic retention times is shown in Figure 2 Figure 2 (a) is the volumetric biogas production rate; (b) is the average biogas production rate. From Figure 2 ​​As can be seen from (a) in Table 1, the volumetric biogas production rate in the reactor showed a gradual upward trend with the shortening of HRT and the increase of OLR. During the start-up period of 10 days, the volumetric biogas production rate fluctuated between 93.00-145.10 mL / L / d, indicating that the reactor was relatively stable. When the OLR was gradually increased to 1.67 g TS / L / d (HRT=30 d), 2.50 g TS / L / d (HRT=20 d) and 5.00 g TS / L / d (HRT=10 d), the volumetric biogas production rate also increased, with the average values being 311.40 mL / L / d, 394.64 mL / L / d and 856.3 mL / L / d, respectively. However, from (b) in Table 1, it can be found that when the HRT was 30 d, the biogas production per unit mass of raw material in the reactor was the maximum among all experimental groups, being 186.91 mL / g TS. When the HRT was shortened to 20 d and 10 d, the average biogas production decreased to 157.86 mL / g TS and 165.65 mL / g TS, respectively. This indicates that by shortening the HRT, the volumetric biogas production rate can be increased while the process cycle is shortened, and the material disposal efficiency is improved. However, too high OLR will reduce the average time of contact between the material and microorganisms, and reduce the conversion rate of the material and the biogas production efficiency, because a larger OLR leads to insufficient stirring of fresh material and old material in the reactor, which in turn causes part of the substrate to be not fully converted and utilized before being discharged the next day. In the conventional fermentation process, a higher OLR increases the volumetric biogas production rate and improves the material disposal efficiency, but too high OLR reduces the conversion rate of the material and produces biogas residue that cannot be utilized, resulting in waste. In the present system, the biogas residue is used as raw material for gasification, effectively solving this problem. Figure 2

[0040] Example 2

[0041] In this example, the system in Example 1 and the biogas and biogas residue produced by the system are used.

[0042] The biogas is transported to the front of the gasification reactor inlet valve through the biogas compression temporary storage tank; the water vapor generated by the water vapor generator is pre-mixed with the biogas and then transported through the gasification reactor; the biogas residue is transported through the separation dryer and then fed into the screw feeder; the biogas residue in the screw feeder is transported into the gasification reactor, and the water vapor, biogas and biogas residue perform hydrogen production reaction in the gasification reactor to obtain the gasification product.

[0043] ​In the basket evenly into 6 g of biogas residue, the basket is lifted to the highest. When the temperature rises to 800℃, the iron rod hanging the raw material basket is lowered, the raw material enters the furnace, the gasification of biogas residue is carried out, at the same time, the gas bag is connected, the whole gasification process lasts for 20 min. The flow of N2 is 200 ml / min during the whole experiment. Because there is no water vapor, the mass ratio of water vapor to biogas residue is 0, which is recorded as S / B=0. After 20 min, the equipment stops running, and cools down by itself, at the same time, the gas bag is taken out, and the gas collection is completed. The gas produced in the gasification process passes through the condensing equipment and the wet flow meter in turn, and is finally collected by the gas bag. The obtained gas is detected by gas chromatography to obtain the concentrations of H2, CO, CO2 and CH4 in the product, and the concentration of each gas is calculated. The hydrogen yield under this condition is 75.07 mL / g.

[0044] Example 3

[0045] In this example, the conditions of hydrogen production reaction are changed compared with example 2, which are as follows: In the basket evenly into 6 g of biogas residue, the basket is lifted to the highest. When the temperature rises to 800℃, the iron rod hanging the raw material basket is lowered, the raw material enters the furnace, the gasification of biogas residue is carried out, at the same time, the gas bag is connected, the whole gasification process lasts for 20 min. The flow of N2 is 200 ml / min during the whole experiment. Because there is no water vapor, the mass ratio of water vapor to biogas residue is 0, which is recorded as S / B=0. After 20 min, the equipment stops running, and cools down by itself, at the same time, the gas bag is taken out, and the gas collection is completed. The gas produced in the gasification process passes through the condensing equipment and the wet flow meter in turn, and is finally collected by the gas bag. The obtained gas is detected by gas chromatography to obtain the concentrations of H2, CO, CO2 and CH4 in the product, and the concentration of each gas is calculated. The hydrogen yield under this condition is 75.07 mL / g. Figure 3 The hydrogen yield of example 2 and example 3 is shown in the table, compared with example 2, the hydrogen yield is increased by 1.97 times, and the H2 content is increased significantly, which shows that the water gas reaction is enhanced with the introduction of water vapor, and the hydrogen content is increased to synthesize high-quality synthesis gas.

[0046] Example 4

[0047] In this example, the conditions of hydrogen production reaction are changed compared with example 2, which are as follows: In the basket, evenly spread into 6 g of biogas residue, the basket is lifted to the highest place. When the temperature rises to 800℃, the iron rod hanging the raw material basket is lowered, the raw material enters the furnace, and the gasification of the biogas residue is carried out, and at the same time, the gas bag is connected. The whole gasification process lasts for 20 min. During the whole experiment, the mixed biogas atmosphere of N2 with a flow rate of 50 ml / min and biogas with a flow rate of 150 ml / min is continuously introduced (S / B=0). After 20 min, the equipment stops running, and the gas bag is taken out after cooling down. The gas produced in the gasification process is collected by the gas bag after passing through the condensation equipment and the wet flow meter in turn. The obtained gas is detected by gas chromatography to obtain the concentrations of H2, CO, CO2 and CH4 in the product, and the concentration of each gas is calculated. According to the experimental results, it can be known that the H2 produced under this condition is 95.20 ml / g.

[0048] Example 5

[0049] In this embodiment, the conditions of the hydrogen production reaction are changed compared with Example 4, which are as follows: In the basket, evenly spread into 6 g of biogas residue, the basket is lifted to the highest place. When the temperature rises to 800℃, the iron rod hanging the raw material basket is lowered, the raw material enters the furnace, and the gasification of the biogas residue is carried out, and at the same time, the gas bag is connected. The whole gasification process lasts for 20 min. During the whole experiment, the mixed biogas atmosphere of N2 with a flow rate of 50 ml / min and biogas with a flow rate of 150 ml / min is continuously introduced (S / B=0). After 20 min, the equipment stops running, and the gas bag is taken out after cooling down. The gas produced in the gasification process is collected by the gas bag after passing through the condensation equipment and the wet flow meter in turn. The obtained gas is detected by gas chromatography to obtain the concentrations of H2, CO, CO2 and CH4 in the product, and the concentration of each gas is calculated. According to the experimental results, it can be known that the H2 produced under this condition is 95.20 ml / g. Figure 4 As shown in the table, compared with Example 4, the hydrogen production is increased by 2.62 times, and the hydrogen content H2 is significantly increased, which shows that the steam introduction enhances the methane wet reforming, increases the hydrogen content, and thus synthesizes high-quality synthesis gas.

[0050] As shown in the table, compared with Example 4, the hydrogen production is increased by 2.62 times, and the hydrogen content H2 is significantly increased, which shows that the steam introduction enhances the methane wet reforming, increases the hydrogen content, and thus synthesizes high-quality synthesis gas. Figure 5 As shown in the table, compared with Example 4, the hydrogen production is increased by 2.62 times, and the hydrogen content H2 is significantly increased, which shows that the steam introduction enhances the methane wet reforming, increases the hydrogen content, and thus synthesizes high-quality synthesis gas.

[0051] Example 6

[0052] The difference between Example 6 and Example 5 is that the flow rate of water vapor is 0.3ml / min, at this time S / B=1, under this condition, H2 is 134.38ml / g.

[0053] Example 7

[0054] The difference between Example 7 and Example 5 is that the flow rate of water vapor is 0.9ml / min, at this time S / B=3, under this condition, H2 is 288.00ml / g.

[0055] Example 8

[0056] The difference between Example 8 and Example 5 is that the flow rate of water vapor is 1.2ml / min, at this time S / B=4, under this condition, H2 is 319.61ml / g.

[0057] The hydrogen production and proportion of Example 4, Example 5, Example 6, Example 7 and Example 8 are shown in the table as follows: Figure 6 As can be seen from the table, with the gradual increase of S / B, the hydrogen production and concentration gradually increase, compared with S / B=0, the hydrogen production is increased by 0.41, 1.62, 2.02 and 2.36 respectively; the hydrogen proportion is 10.01%, 12.94%, 18.56%, 19.05% and 20.77% respectively. Due to the overlapping effect of water gas reaction and methane wet reforming, when S / B is in the range of 0-2, the hydrogen amount and hydrogen concentration increase faster, but due to the increase of water vapor, the heat balance is destroyed, the temperature drops, which obviously makes the growth in the range of 2-4 relatively flat, but still increases. The system design breaks through the disadvantage of extremely low H / C of biogas residue, produces a large amount of H2, which is beneficial to the production of clean energy, and has great application potential in efficient green hydrogen energy production.

[0058] The present application introduces biogas as a gasifying agent and water vapor as an oxidizing body, which can significantly improve the hydrogen production of biogas residue gasification. First, in the biogas atmosphere, CH4 and CO2 can enhance the dry reforming hydrogen production reaction, and the synergistic effect is more obvious. Second, the introduced water vapor, as an excellent oxidizing body, not only can convert more biochar and tar into small molecule syngas, but also can enhance hydrogen production. Compared with traditional biomass gasification, the multi-source atmosphere gasification method under anaerobic fermentation mediation can effectively improve the conversion rate of raw materials and hydrogen production efficiency.

[0059] The above only describes the preferred embodiments of the present application, and it should be pointed out that for ordinary skilled persons in the art, without departing from the principles of the present application, a number of improvements and refinements can be made, which should also be considered as the protection scope of the present application.

Claims

1. An anaerobic fermentation mediated biomass polygeneration atmosphere gasification hydrogen production system, characterized in that, The device comprises a full-mixing continuous anaerobic reactor, a biogas compression temporary storage tank, a separation dryer, a water vapor transmitter, a screw feeder, a gasification reaction bed, a cyclone separator, and a hydrogen purification column.

2. The anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 1, wherein, The full-mixing continuous anaerobic reactor is connected with the biogas compression temporary storage tank through a gas outlet, and is connected with the separation dryer through a residue outlet.

3. The anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 2, wherein, The separation dryer is connected with the screw feeder, and the gasification reaction bed is connected with the biogas compression temporary storage tank, the water vapor transmitter and the screw feeder.

4. The anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 3, wherein, The gasification reaction bed is connected with the hydrogen purification column through the cyclone separator.

5. The operation method of the system for hydrogen production from biomass gasification in a multi-source atmosphere mediated by anaerobic fermentation according to any one of claims 1 to 4, characterized in that, The device comprises the following steps: (1) biogas obtained by anaerobic fermentation in the full-mixing continuous anaerobic reactor is transported to the front of a gas inlet valve of the gasification reaction bed through the biogas compression temporary storage tank; water vapor generated by the water vapor transmitter is premixed with the biogas and then transported into the gasification reaction bed; (2) biogas residue generated by the full-mixing continuous anaerobic reactor is transported into the screw feeder through the separation dryer; the biogas residue in the screw feeder is transported into the gasification reaction bed; (3) water vapor, biogas and biogas residue are subjected to a hydrogen production reaction in the gasification reaction bed to obtain a gasification product; the gasification product is transported into the hydrogen purification column through the cyclone separator to obtain hydrogen, and the operation is completed.

6. The operation method of the anaerobic fermentation-mediated biomass multi-source gas atmosphere gasification hydrogen production system according to claim 5, characterized in that, The total solid concentration of the reaction raw material in the anaerobic fermentation in step (1) is 4-6%.

7. The method of operating an anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 6 wherein, The reaction temperature of the anaerobic fermentation in step (1) is 35-55℃, and the hydraulic retention time is 10-30 days.

8. The operation method of the anaerobic fermentation-mediated biomass multi-source gas atmosphere gasification hydrogen production system according to claim 7, characterized in that, The mass ratio of water vapor to biogas residue in the hydrogen production reaction in step (3) is ≤8.

9. The method of operating an anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 8 wherein, The carrier gas flow rate in the hydrogen production reaction in step (3) is 100-300 mL / min.

10. The method of operating an anaerobic fermentation mediated biomass multi-feed gas atmosphere gasification hydrogen production system as claimed in claim 9 wherein, The gasification temperature in the hydrogen production reaction in step (3) is 700-900℃, and the time is 10-60 min.

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