System for hydrogen production by supercritical water gasification of biomass

Abstract

The utility model discloses a kind of biomass supercritical water gasification hydrogen production systems, belong to biomass hydrogen production technical field, to realize low-cost hydrogen production, the biomass supercritical water gasification hydrogen production system includes raw material tank (1), feed pump (2), reaction furnace (3), cooler (4), gas-liquid separator (5), lye pool (6), waste liquid tank (7) and product tank (8), raw material tank (1), feed pump (2), reaction furnace (3), cooler (4) and gas-liquid separator (5) are sequentially connected.The biomass supercritical water gasification hydrogen production system uses discarded biomass raw material, without being subjected to complex processing technology, device is simple, compared with traditional water electrolysis hydrogen production, low investment, low cost.

Description

Technical Field

[0001] This utility model relates to the field of biomass hydrogen production technology, specifically a system for producing hydrogen through supercritical water gasification of biomass. Background Technology

[0002] The concept of hydrogen metallurgy was first proposed in the 20th century. It involves using hydrogen to reduce iron ore instead of carbon, thereby fundamentally reducing emissions of pollutants at the source. Currently, the mainstream hydrogen metallurgy technologies are blast furnace hydrogen-enriched smelting and gas-based direct reduction shaft furnace ironmaking.

[0003] The concept of hydrogen metallurgy is still in its early stages, both theoretically and practically, and faces numerous challenges. The biggest challenge remains the low-cost hydrogen production problem. Currently, most steel companies aim to utilize coke oven gas and other sources for hydrogen smelting projects, and related research and development is in its early stages. Hydrogen production processes and hydrogen metallurgy technologies require breakthroughs in key technologies, and the future of hydrogen metallurgy still needs continuous exploration. Utility Model Content

[0004] To achieve low-cost hydrogen production, this invention provides a system for producing hydrogen through supercritical water gasification of biomass. The system uses waste biomass raw materials, requires no complex processing, has a simple setup, and has lower investment and cost compared to traditional water electrolysis for hydrogen production.

[0005] The technical solution adopted by this utility model embodiment to solve its technical problem is:

[0006] A system for producing hydrogen from biomass supercritical water gasification includes a feed tank, a feed pump, a reactor, a cooler, a gas-liquid separator, an alkali tank, a waste liquid tank, and a product tank. The feed tank, feed pump, reactor, cooler, and gas-liquid separator are connected in sequence. The gas outlet of the gas-liquid separator is connected to the gas inlet of the alkali tank, the gas outlet of the alkali tank is connected to the inlet of the product tank, and the liquid outlet of the gas-liquid separator is connected to the inlet of the waste liquid tank.

[0007] The reactor is a vertical cylindrical structure with a raw material inlet and a reactant outlet. The reactor contains a reaction chamber. During operation, the reaction temperature in the reaction chamber is 400℃~600℃ and the reaction pressure in the reaction chamber is 22.4MPa~25MPa.

[0008] The raw material inlet is located at the bottom of the reactor, and the reactant outlet is located at the top of the reactor. Both the raw material inlet and the reactant outlet are connected to the reaction chamber.

[0009] The reactor contains an inner shell and an outer shell, both of which are upright cylindrical structures. The reaction cavity is located inside the inner shell, and an annular outer cavity is formed between the inner shell and the outer shell.

[0010] The annular outer cavity is equipped with heating elements and insulation material. The heating elements are heating wires, and the reaction inner cavity is equipped with temperature measuring elements.

[0011] The reaction chamber is equipped with helical blades, the axis of which coincides with the axis of the reactor, forming a spiral upward channel in the reaction chamber.

[0012] Along the upward direction, the pitch of the helical blades gradually increases.

[0013] The cooler has an exothermic medium inlet, an exothermic medium outlet, an endothermic medium inlet, and an endothermic medium outlet. The reactant outlet of the reactor is connected to the exothermic medium inlet of the cooler. The cooler can cool the reaction products discharged from the reactor to 20℃~30℃. The exothermic medium outlet of the cooler is connected to the inlet of the gas-liquid separator through a conveying pipeline.

[0014] The delivery pipeline is equipped with a pressure regulating valve assembly, which contains multiple pressure reducing valves connected in series. The pressure regulating valve assembly can reduce the pressure from 22.4MPa to 25MPa to 16MPa.

[0015] The gas-liquid separator is a cyclone type. The gas outlet of the gas-liquid separator is located at the top, and the liquid outlet is located at the bottom. The gas inlet of the alkali solution tank is located at the bottom and below the alkali solution surface. The gas outlet of the alkali solution tank is located at the top and above the alkali solution surface. A gas pressurization device is installed between the gas outlet of the alkali solution tank and the inlet of the product tank.

[0016] The beneficial effects of this utility model embodiment are:

[0017] 1. It uses waste biomass raw materials, without the need for complicated processing. The equipment is simple and has lower investment and cost compared with traditional water electrolysis for hydrogen production.

[0018] 2. Using wet biomass or biomass waste liquid, compared with other biomass hydrogen production processes, there is no need to heat and dry the biomass, thus reducing energy consumption.

[0019] 3. The continuous flow reactor is adopted, which makes it easier to control the temperature, makes it easier to form laminar flow inside, and has a better heat transfer effect.

[0020] 4. The reaction leaves less residual biomass waste liquid, resulting in less environmental pollution compared to other processes. Attached Figure Description

[0021] The accompanying drawings, which form part of this application, are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention.

[0022] Figure 1 This is a schematic diagram of the biomass supercritical water gasification hydrogen production system described in this utility model.

[0023] Figure 2 This is a schematic diagram of the reactor.

[0024] Figure 3 This is a schematic diagram of the cooler.

[0025] Figure 4 This is a schematic diagram of a gas-liquid separator.

[0026] Figure 5 This is a schematic diagram of an alkali solution tank.

[0027] Figure 6 This is a schematic diagram of a waste liquid tank.

[0028] Figure 7 This is a schematic diagram of the product can.

[0029] Figure 8 This is a schematic diagram of a pressure regulating valve assembly.

[0030] The annotations in the attached figures are explained as follows:

[0031] 1. Raw material tank; 2. Feed pump; 3. Reactor; 4. Cooler; 5. Gas-liquid separator; 6. Alkali solution tank; 7. Waste liquid tank; 8. Product tank; 9. Pressure regulating valve assembly;

[0032] 301. Raw material inlet; 302. Reactant outlet; 303. Reaction chamber; 304. Insulation material; 305. Inner shell; 306. Outer shell; 307. Annular outer cavity; 308. Heating component; 309. Helical blades;

[0033] 401. Inlet for exothermic medium; 402. Outlet for exothermic medium; 403. Inlet for absorbent medium; 404. Outlet for absorbent medium; 405. Delivery pipeline;

[0034] 501. Gas outlet of the gas-liquid separator; 502. Liquid outlet of the gas-liquid separator;

[0035] 601. Gas inlet of the alkali solution tank; 602. Gas outlet of the alkali solution tank;

[0036] 701. Inlet of the waste liquid tank;

[0037] 801. Inlet of the product tank;

[0038] 901. Pressure reducing valve. Detailed Implementation

[0039] It should be noted that, unless otherwise specified, the embodiments and features described in this application can be combined with each other. The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0040] For ease of understanding and description, the following description of this utility model uses absolute positional relationships. Unless otherwise specified, the directional word "above" indicates... Figure 1 The direction above, the directional word "down" indicates Figure 1 The lower side of the middle, "left" indicates Figure 1 The left side of the direction, the directional word "right" indicates Figure 1 The right-hand direction in the middle, "front" means perpendicular to Figure 1 The direction of the paper and the direction pointing inwards; the directional word "back" indicates perpendicular to. Figure 1 The orientation of the paper is pointed outwards from the viewpoint of the reader or user. This invention is described from the perspective of the reader or user, but the aforementioned directional terms should not be construed as limiting the scope of protection of this invention. Regarding the dimensions, angles, and parameters of the components, those skilled in the art can determine or replace them according to actual needs or a limited number of experiments.

[0041] like Figure 1 As shown in the embodiment of this utility model, a biomass supercritical water gasification hydrogen production system includes a raw material tank 1, a feed pump 2, a reactor 3, a cooler 4, a gas-liquid separator 5, an alkali tank 6, a waste liquid tank 7, and a product tank 8. The raw material tank 1, feed pump 2, reactor 3, cooler 4, and gas-liquid separator 5 are connected in sequence. The gas outlet 501 of the gas-liquid separator is connected to the gas inlet 601 of the alkali tank, the gas outlet 602 of the alkali tank is connected to the inlet 801 of the product tank, and the liquid outlet 502 of the gas-liquid separator is connected to the inlet 701 of the waste liquid tank.

[0042] like Figure 2 As shown, the reactor 3 is a continuous flow reactor. The reactor 3 can be a vertical cylindrical structure. The reactor 3 is provided with a raw material inlet 301 and a reactant outlet 302 (also called a reaction product outlet). The reactor 3 contains a closed reaction chamber 303. During operation, the reaction temperature in the reaction chamber 303 can be 400℃~600℃ (preferably 550℃), and the reaction pressure in the reaction chamber 303 can be 22.4MPa~25MPa.

[0043] The raw material inlet 301 is located at the lower part of the reactor 3, and the reactant outlet 302 is located at the upper part (such as the top) of the reactor 3. Both the raw material inlet 301 and the reactant outlet 302 are connected to the reaction chamber 303. The reactants can enter the reaction chamber 303 through the raw material inlet 301 and react, and the reaction products can be discharged through the reactant outlet 302.

[0044] like Figure 2 As shown, the reactor 3 includes an inner shell 305 and an outer shell 306, which are separated by an inner shell. Both the inner shell 305 and the outer shell 306 are upright cylindrical structures. The reaction cavity 303 is located inside the inner shell 305, and a closed annular outer cavity 307 is formed between the inner shell 305 and the outer shell 306.

[0045] A heating element 308 and insulation material 304 are disposed within the annular outer cavity 307. The heating element 308 can be a heating wire, and a temperature measuring element is disposed within the reaction cavity 303. The heating element 308 is used to heat the reaction cavity 303, and the temperature measuring element can be a thermocouple to measure the temperature within the reaction cavity 303. The insulation material 304 can be made of rock wool or glass wool.

[0046] like Figure 2 As shown, a spiral blade 309 is provided in the reaction chamber 303. The axis of the spiral blade 309 coincides with the axis of the reactor 3, and the spiral blade 309 forms a spiral ascending channel in the reaction chamber 303. After the reactants enter the reaction chamber 303, they rise along the spiral ascending channel to ensure that the reactants can react fully.

[0047] To avoid potential dead zones in the reaction chamber 303, the helical blades 309 can be connected to a drive motor. The drive motor can drive the helical blades 309 to rotate continuously around the axis of the reactor 3. The rotation direction of the helical blades 309 is such that the reactants in the reaction chamber 303 move from bottom to top. The drive motor is located outside the lower end of the reactor 3.

[0048] To ensure the reactants are fully heated and thus achieve a more complete reaction, the pitch of the spiral blades 309 gradually increases from bottom to top. This allows the reactants to gradually decrease in speed as they ascend along the spiral channel after entering the reaction chamber 303.

[0049] like Figure 3As shown, the cooler 4 includes an exothermic medium inlet 401, an exothermic medium outlet 402, an endothermic medium inlet 403, and an endothermic medium outlet 404. The reactant outlet 302 of the reactor 3 is connected to the exothermic medium inlet 401 of the cooler 4. The cooler 4 can cool the reaction products discharged from the reactor 3 to 20°C to 30°C. The exothermic medium outlet 402 of the cooler 4 is connected to the inlet of the gas-liquid separator 5 through a conveying pipeline 405.

[0050] The heat-absorbing medium inlet 403 is connected to the cooling water inlet pipeline, and the heat-absorbing medium outlet 404 is connected to the cooling water outlet pipeline. The reaction product enters the cooler 4 from the heat-releasing medium inlet 401 and releases heat. After the reaction product releases heat, it is discharged from the heat-releasing medium outlet 402. The temperature of the reaction product discharged from the heat-releasing medium outlet 402 is 20℃~30℃.

[0051] like Figure 1 and Figure 8 As shown, due to the extremely high pressure in the reactor 3, the pressure of the reaction products after cooling is still very high. In order to facilitate further processing of the reaction products, a pressure regulating valve group 9 is installed on the conveying pipeline 405. The pressure regulating valve group 9 contains multiple pressure reducing valves 901 connected in series. The pressure regulating valve group 9 can reduce the pressure from 22.4MPa to 25MPa to 16MPa.

[0052] The heat release medium outlet 402 of the cooler 4 is connected to the inlet of the gas-liquid separator 5 through two conveying pipelines 405. The two conveying pipelines 405 are arranged in parallel, and each of the two conveying pipelines 405 can be equipped with a pressure regulating valve assembly 9, which contains multiple pressure reducing valves 901 connected in series. In this way, when the pressure regulating valve assembly 9 on one conveying pipeline 405 fails, the pressure regulating valve assembly 9 on the other conveying pipeline 405 can still operate.

[0053] like Figure 4 As shown, the gas-liquid separator 5 can be an existing cyclone gas-liquid separator. The gas outlet 501 of the gas-liquid separator is located at the upper part (such as the top) of the gas-liquid separator 5, and the liquid outlet 502 of the gas-liquid separator is located at the lower part of the gas-liquid separator 5. The alkali tank 6 can be a closed tank containing alkali solution. The gas inlet 601 of the alkali tank is located at the lower part of the alkali tank 6 and below the surface of the alkali solution in the alkali tank 6. The gas outlet 602 of the alkali tank is located at the upper part of the alkali tank 6 and above the surface of the alkali solution in the alkali tank 6.

[0054] like Figure 1 , Figure 4 , Figure 5 , Figure 6 and Figure 7As shown, the crude gas separated by the gas-liquid separator 5 is passed into the alkali tank 6 to remove residual acidic gas. A gas pressurization device can be installed between the alkali tank 6 and the product tank 8. The gas (hydrogen) discharged from the alkali tank 6 can enter the gas pressurization device, which pressurizes the hydrogen and then transports it to the product tank 8 for storage. In addition, all components of the biomass supercritical water gasification hydrogen production system can be existing technology products.

[0055] The working process of the biomass supercritical water gasification hydrogen production system is described below.

[0056] 1. Collect the aqueous waste liquid or other liquid biomass waste liquid containing alcohol, ketone, or aldehyde groups generated during the preparation of bio-oil (e.g., biodiesel and / or biogasoline). The reaction raw materials contain carboxylic acids, alcohols, glucose, cellulose, or hemicellulose. After filtering the residue (i.e., the reaction raw materials), store them in raw material tank 1. Compared to other biomass hydrogen production methods, this method eliminates the drying process of wet biomass, reducing the energy consumed in the biomass pretreatment process.

[0057] 2. The biomass liquid (i.e., the reaction raw material) is pumped into the reaction chamber 303 of the reactor 3 using the feed pump 2. The feed pump 2 can be selected in different forms and sizes depending on the amount of liquid pumped in. The temperature in the reaction chamber 303 of the reactor 3 is 600℃, the pressure is 25MPa, and the flow rate is 12kg / h. The residence time of the reaction raw material in the reaction chamber 303 of the reactor 3 is 100s to 1000s. The gaseous products and liquid products (i.e., reaction products) generated by the reaction of the biomass liquid in the reaction chamber 303 enter the cooler 4 from the exothermic medium inlet 401. The cooler 4 cools the reaction products.

[0058] Because the raw material liquid has a complex composition, containing various carboxylic acids, alcohols, and other substances, the main processes of the reaction of the raw materials in the reaction chamber 303 include:

[0059] CH3COOH + 2H2O → 4H2 + 2CO2

[0060] C6H 12 O6 + 6H2O → 6CO2 + 12H2

[0061] HCOOH→CO2+H2

[0062] C2H5OH + H2O → 2H2 + CO2 + CH4

[0063] 3. The cooled reaction products enter the gas-liquid separator 5 for gas-liquid separation. The gas separated in the gas-liquid separator 5 enters the alkaline solution tank 6, and the liquid separated in the gas-liquid separator 5 enters the waste liquid tank 7 for collection.

[0064] 4. The crude gas separated by the gas-liquid separator 5 is passed into the alkaline solution tank 6 to remove residual acidic gas. Then, the purified product hydrogen from the alkaline solution tank 6 is sent to the product tank 8 for storage.

[0065] The biomass supercritical water gasification hydrogen production system uses wet biomass or biomass waste liquid to produce hydrogen, eliminating the need for heating and drying raw materials. This results in low hydrogen production costs and minimal pollution. The system's overall configuration is reasonable and energy-efficient. The optimal operating temperature and pressure within the reaction chamber 303 of reactor 3 are lower than in other supercritical processes, indirectly reducing energy consumption.

[0066] The above description is merely a specific embodiment of this utility model and should not be construed as limiting the scope of its implementation. Therefore, any substitution of equivalent components or equivalent changes and modifications made within the scope of protection of this utility model should still fall within its coverage. Furthermore, the technical features, technical solutions, and embodiments of this utility model can be freely combined and used.

Claims

1. A system for producing hydrogen from biomass through supercritical water gasification, characterized in that, The biomass supercritical water gasification hydrogen production system includes a raw material tank (1), a feed pump (2), a reactor (3), a cooler (4), a gas-liquid separator (5), an alkali tank (6), a waste liquid tank (7), and a product tank (8). The raw material tank (1), feed pump (2), reactor (3), cooler (4), and gas-liquid separator (5) are connected in sequence. The gas outlet (501) of the gas-liquid separator is connected to the gas inlet (601) of the alkali tank. The gas outlet (602) of the alkali tank is connected to the inlet (801) of the product tank. The liquid outlet (502) of the gas-liquid separator is connected to the inlet (701) of the waste liquid tank.

2. The system for producing hydrogen from biomass supercritical water gasification according to claim 1, characterized in that, The reactor (3) is a vertical cylindrical structure. The reactor (3) is provided with a raw material inlet (301) and a reactant outlet (302). The reactor (3) contains a reaction chamber (303). During operation, the reaction temperature in the reaction chamber (303) is 400℃~600℃ and the reaction pressure in the reaction chamber (303) is 22.4MPa~25MPa.

3. The system for producing hydrogen from biomass supercritical water gasification according to claim 2, characterized in that, The raw material inlet (301) is located at the lower part of the reactor (3), and the reactant outlet (302) is located at the upper part of the reactor (3). Both the raw material inlet (301) and the reactant outlet (302) are connected to the reaction chamber (303).

4. The system for producing hydrogen from biomass supercritical water gasification according to claim 2, characterized in that, The reactor (3) contains an inner shell (305) and an outer shell (306) that are separated into inner and outer shells. Both the inner shell (305) and the outer shell (306) are upright cylindrical structures. The reaction cavity (303) is located inside the inner shell (305). An annular outer cavity (307) is formed between the inner shell (305) and the outer shell (306).

5. The system for producing hydrogen from biomass supercritical water gasification according to claim 4, characterized in that, A heating element (308) and insulation material (304) are provided in the annular outer cavity (307). The heating element (308) is an electric heating wire, and a temperature measuring element is provided in the reaction inner cavity (303).

6. The system for producing hydrogen from biomass supercritical water gasification according to claim 2, characterized in that, The reaction chamber (303) is equipped with a spiral blade (309), the axis of which coincides with the axis of the reactor (3), forming a spiral upward channel in the reaction chamber (303).

7. The system for producing hydrogen from biomass supercritical water gasification according to claim 6, characterized in that, Along the upward direction, the pitch of the helical blade (309) gradually increases.

8. The system for producing hydrogen from biomass supercritical water gasification according to claim 2, characterized in that, The cooler (4) includes an exothermic medium inlet (401), an exothermic medium outlet (402), an endothermic medium inlet (403), and an endothermic medium outlet (404). The reactant outlet (302) of the reactor (3) is connected to the exothermic medium inlet (401) of the cooler (4). The cooler (4) can cool the reaction products discharged from the reactor (3) to 20°C to 30°C. The exothermic medium outlet (402) of the cooler (4) is connected to the inlet of the gas-liquid separator (5) through a conveying pipeline (405).

9. The system for producing hydrogen from biomass supercritical water gasification according to claim 8, characterized in that, A pressure regulating valve assembly (9) is installed on the delivery pipeline (405). The pressure regulating valve assembly (9) contains multiple pressure reducing valves (901) connected in series. The pressure regulating valve assembly (9) can reduce the pressure from 22.4MPa to 25MPa to 16MPa.

10. The system for producing hydrogen from biomass supercritical water gasification according to claim 2, characterized in that, The gas-liquid separator (5) is a cyclone gas-liquid separator. The gas outlet (501) of the gas-liquid separator is located at the upper part of the gas-liquid separator (5), and the liquid outlet (502) of the gas-liquid separator is located at the lower part of the gas-liquid separator (5). The gas inlet (601) of the alkali tank is located at the lower part of the alkali tank (6). The gas inlet (601) of the alkali tank is located below the alkali liquid surface in the alkali tank (6). The gas outlet (602) of the alkali tank is located at the upper part of the alkali tank (6). The gas outlet (602) of the alkali tank is located above the alkali liquid surface in the alkali tank (6). A gas pressurization device is provided between the gas outlet (602) of the alkali tank and the inlet (801) of the product tank.

Images