Tail gas utilization system after hydrogen recovery of methanol purge gas
By using the exhaust gas recovered from methanol relaxation hydrogen for solid oxide fuel cell power generation, and combined with CO2 capture, the problems of low methanol relaxation utilization and high carbon emissions are solved, and efficient exhaust gas utilization and near-zero emissions are achieved.
Patent Information
- Application Number
- CN202421982831.9
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-08-16
- Publication Date
- 2025-08-15
- Estimated Expiration
- 2034-08-16
AI Technical Summary
In the existing IGFC technology, the high concentration of syngas produced by coal gasification is poor in power generation as fuel, and the exhaust gas utilization rate of methanol relaxation hydrogen recovery is low, and the CO2 concentration is low after combustion is not easy to catch, resulting in high carbon emissions.
The exhaust gas recovered from methanol relaxation hydrogen is used as fuel for solid oxide fuel cells to generate electricity, and electrochemical reactions are carried out through the gas supply unit and the oxygen supply unit, and combined with the CO2 capture device, the recycling and utilization of high concentrations of CO2 in the exhaust gas is realized.
It improves the utilization rate of methanol relaxation gas, reduces carbon emissions, achieves near-zero emissions, and simplifies the process flow and reduces costs.
Smart Images
Figure CN223230351U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of energy development and energy conversion, in particular to a system for utilizing tail gas after hydrogen recovery from methanol purge gas. Background Art
[0002] Integrated Gasification Fuel Cell (IGFC) is a clean and efficient green coal-fired power generation technology. When combined with CO2 capture technology, it can achieve a high power generation efficiency of over 60% and near-zero CO2 emissions. IGFC mainly includes three modules: coal gasification and purification, fuel cell power generation, and exhaust gas combustion waste heat recovery. The mixture of CO2 and H2O obtained from combustion can be coupled with CO2 capture and storage technology. The general process of IGFC is as follows (see Figure 1 ): Coal (or natural gas, biomass, etc.) is gasified to generate synthesis gas. After heat recovery, the synthesis gas enters a purification unit to remove harmful substances such as sulfur and dust. The purified gas is fed into the anode side of a high-temperature fuel cell (including solid oxide fuel cells (SOFCs) and molten carbonate fuel cells (MCFCs). Simultaneously, air is introduced into the cathode side. The fuel gas and oxidizing gas undergo an electrochemical reaction within the cell to generate electricity. During the reaction, most of the combustible components are converted into electricity and heat. The unconverted combustible components are discharged with the cell's anode exhaust and enter the combustion chamber for catalytic combustion, where they are completely converted into CO2 and H2O. After heat recovery and condensation of H2O from this mixed gas, CO2 gas with a purity of over 90% is obtained, which can be directly captured and stored.
[0003] Existing IGFC technology uses high-concentration syngas (CO+H2) produced by coal gasification as fuel for high-temperature fuel cell power generation. This solution is suitable for large-scale coal-fired power plants. However, for traditional coal chemical companies, high-concentration syngas (CO+H2) is a key chemical feedstock for producing chemical products such as methanol, dimethyl ether, and acetic acid. However, its production cost is high, and its direct use as fuel for power generation is uneconomical.
[0004] For traditional coal chemical enterprises, the synthesis gas (CO+H2) produced by coal gasification is mostly used to synthesize chemical products such as methanol. The typical process flow is as follows (see Figure 2 ): The crude synthesis gas produced by coal gasification undergoes a conversion reaction (CO+H2O=CO2+H2) and enters low-temperature methanol to wash out impurities such as CO2, H2S, organic sulfur (COS, CS2) in the crude coal gas, and obtains clean coal gas as methanol synthesis gas for methanol synthesis. After methanol synthesis, the remaining raw gas is used as circulating gas for methanol synthesis in one way, and the other way is relaxation gas that passes through a hydrogen recovery device to obtain rich hydrogen. The remaining tail gas enters the fuel gas pipeline network.
[0005] The existing utilization routes of tail gas from methanol purge gas hydrogen recovery are: 1) venting to the flare for hydrogen recovery; 2) desulfurization recovery and co-firing in the combustion furnace; 3) burning in the flare as a permanent lamp; 4) burning in the boiler.
[0006] The H2 content in methanol purge gas is above 70% and does not contain sulfides. The content of combustible gas (H2+CO+CH4) in the tail gas after hydrogen recovery is above 60%. The fuel utilization rate when transported to the boiler for combustion is low and the CO2 concentration after combustion is low and difficult to capture. Utility Model Content
[0007] The purpose of the utility model is to provide a methanol purge gas tail gas utilization system after hydrogen recovery to solve the problems existing in the above-mentioned prior art, use the tail gas of methanol purge gas as fuel for solid oxide fuel cell to generate electricity, improve the utilization rate of the purge gas, and recover and utilize the high concentration of CO2 in the tail gas after the reaction, so as to achieve the purpose of reducing carbon emissions.
[0008] To achieve the above purpose, the present invention provides the following solutions:
[0009] A methanol purge gas hydrogen recovery tail gas utilization system, comprising a solid oxide fuel cell, a gas supply unit and an oxygen supply unit;
[0010] The gas supply unit includes a methanol synthesis device, a hydrogen recovery device, a preheating device and a methane reforming reaction device which are connected in sequence;
[0011] The methane reforming reaction device includes a reaction chamber for performing a reforming reaction and a combustion chamber for providing heat for the reforming reaction, wherein the outlet of the reaction chamber is connected to the anode inlet of the solid oxide fuel cell, the anode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber, and the outlet of the combustion chamber is connected to a CO2 capture device;
[0012] The oxygen supply unit includes an oxygen supply source and a heat exchange device connected in sequence, the cold side outlet of the heat exchange device is connected to the cathode inlet of the solid oxide fuel cell, and the cathode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber.
[0013] Preferably, the outlet of the hydrogen recovery device is communicated with the inlet of the combustion chamber.
[0014] Preferably, the outlet of the oxygen supply source is communicated with the inlet of the combustion chamber.
[0015] Preferably, the oxygen supply source is an air compressor or a blower.
[0016] Preferably, the cathode outlet of the solid oxide fuel cell is communicated with the hot side inlet of the heat exchange device, and the hot side outlet of the heat exchange device is communicated with the inlet of the combustion chamber.
[0017] Preferably, a waste heat recovery device is provided between the combustion chamber and the CO2 capture device.
[0018] Preferably, the waste heat recovery device is connected to the preheating device.
[0019] Compared with the prior art, the utility model has achieved the following technical effects:
[0020] 1. Compared with the traditional IGFC technology, the present invention does not directly use high-value-added high-concentration synthesis gas to generate electricity. Instead, it uses the tail gas recovered from methanol purge gas with hydrogen, which has a lower recovery value, to generate electricity. Taking a chemical plant with an annual output of 600,000 tons of methanol as an example, the fuel contained in the tail gas after methanol purge gas hydrogen recovery can generate a power of about 3510kW per hour, which is realistic and feasible. In addition, the tail gas recovered from methanol purge gas with hydrogen does not require dust removal, desulfurization and other processes, and the process is simple and low-cost.
[0021] 2. Compared with the traditional tail gas treatment method - tail gas combustion for heat supply, the CO2 generated by this utility model is very concentrated, easy to capture and utilize, which can greatly reduce carbon reduction costs and achieve near-zero carbon dioxide emissions; taking a chemical plant with an annual output of 600,000 tons of methanol as an example, according to this solution, carbon dioxide emissions can be reduced by approximately 1,251 kg per hour. BRIEF DESCRIPTION OF THE DRAWINGS
[0022] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the following briefly introduces the drawings required for use in the embodiments. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.
[0023] Figure 1 This is a typical flow chart of the IGFC system;
[0024] Figure 2 This is a typical process flow chart for methanol synthesis;
[0025] Figure 3 This is a schematic structural diagram of the tail gas utilization system after hydrogen recovery from methanol purge gas disclosed in the utility model;
[0026] Figure 4 This is a diagram of the working principle of SOFC. DETAILED DESCRIPTION
[0027] The following will clearly and completely describe the technical solutions in the embodiments of the present invention in conjunction with the accompanying drawings. People familiar with the art can easily understand the other advantages and functions of the present invention from the content disclosed in this specification. Obviously, the described embodiments are only some of the embodiments of the present invention, not all of them. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without making creative efforts are within the scope of protection of the present invention.
[0028] It should be noted that the structures, proportions, sizes, etc. depicted in the drawings of this specification are only used to match the contents disclosed in the specification, so as to facilitate understanding and reading by those familiar with this technology. They are not intended to limit the conditions under which the present invention can be implemented, and therefore have no technical significance. Any structural modifications, changes in proportional relationships, or adjustments in size should still fall within the scope of the technical content disclosed in this utility model without affecting the effects and objectives that can be achieved by the present utility model. In the description of this utility model, it should be understood that the terms "longitudinal", "transverse", "upper", "lower", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicating directions or positional relationships, are based on the directions or positional relationships shown in the drawings, and are only for the convenience of describing the utility model, and do not indicate or imply that the devices or components referred to must have a specific orientation, be constructed and operate in a specific orientation. Therefore, they should not be understood as limiting the present utility model. In addition, the terms "first", "second", "third", etc. are used for descriptive purposes only and should not be understood as indicating or implying relative importance. Thus, features defined as "first", "second", etc. may explicitly or implicitly include one or more of the features. In the description of the present invention, unless otherwise specified, "plurality" means two or more.
[0029] It should also be noted that in the embodiments of the present application, the same figure mark represents the same component or the same part.
[0030] The purpose of the utility model is to provide a methanol purge gas tail gas utilization system after hydrogen recovery, so as to solve the problems existing in the prior art, use the tail gas of methanol purge gas as fuel for solid oxide fuel cell to generate electricity, improve the utilization rate of the purge gas, and recover and utilize the high concentration of CO2 in the tail gas after the reaction, so as to achieve the purpose of reducing carbon emissions.
[0031] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, the present invention is further described in detail below with reference to the accompanying drawings and specific implementation methods.
[0032] Please refer to Figure 3This embodiment provides a system for utilizing tail gas after hydrogen recovery from methanol purge gas. Combining the IGFC technical ideas and the current production status of coal chemical enterprises, the tail gas recovered from methanol purge gas hydrogen is used as fuel for solid oxide fuel cells to generate electricity, and the high concentration of CO2 in the tail gas after the reaction is recovered and utilized, thereby reducing carbon emissions. Specifically, it includes a solid oxide fuel cell, a gas supply unit, and an oxygen supply unit; the gas supply unit includes a methanol synthesis device, a hydrogen recovery device, a preheating device, and a methane reforming reaction device connected in sequence; the methane reforming reaction device includes a reaction chamber for a reforming reaction and a combustion chamber for providing heat for the reforming reaction, the outlet of the reaction chamber is connected to the anode inlet of the solid oxide fuel cell, the anode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber, and the outlet of the combustion chamber is connected to a CO2 capture device; the oxygen supply unit includes an oxygen supply source and a heat exchange device connected in sequence, the cold side outlet of the heat exchange device is connected to the cathode inlet of the solid oxide fuel cell, and the cathode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber.
[0033] As a preferred solution of this embodiment, the outlet of the hydrogen recovery device is connected to the inlet of the combustion chamber to provide fuel gas to the combustion chamber; the outlet of the oxygen supply source is connected to the inlet of the combustion chamber to provide oxygen to the combustion chamber.
[0034] The cathode outlet of the solid oxide fuel cell is connected to the hot side inlet of the heat exchange device to recover the reaction heat of the solid oxide fuel cell; the hot side outlet of the heat exchange device is connected to the inlet of the combustion chamber to reuse the cathode tail gas of the solid oxide fuel cell.
[0035] A waste heat recovery device is provided between the combustion chamber and the CO2 capture device to recover the heat energy of the combustion chamber. The waste heat recovery device is connected to the preheating device to utilize the recovered heat energy.
[0036] The working process of this embodiment is as follows: a portion of the gas after the reaction of the methanol synthesis unit is returned to the methanol synthesis unit as a circulating gas, and at the same time, a portion is required to be released as a purge gas. The methanol purge gas contains combustible gases such as hydrogen and methane, wherein the hydrogen content is generally above 70%. The hydrogen-rich gas obtained after hydrogen recovery is merged into the clean coal gas and continued to be used for methanol synthesis. The remaining tail gas is divided into two paths: one path of tail gas is directly sent to the combustion chamber of the methane reforming unit for fuel combustion to provide heat for the methane reforming reaction; the other path is heated by the preheating device using the recovered waste heat (low-pressure steam can be used to provide heat in the initial stage) and then enters the methane reforming unit to reform the methane into a mixed gas CO+H2. The reformed mixed gas enters the anode of the solid oxide fuel cell as fuel to undergo an electrochemical reaction, converting CO and H2 into CO2 and water. The fuel tail gas after the reaction is sent to the combustion chamber of the methane reforming unit as fuel for combustion to provide heat for the reforming reaction.
[0037] In this embodiment, the oxygen supply source is preferably an air compressor or blower. After being pressurized by the compressor or blower, the air is split into two paths: one path enters the methane reformer to provide oxygen for the combustion chamber; the other path is heated by a heat exchanger and enters the cathode of the solid oxide fuel cell. The exhaust gas from the reaction is recovered by the heat exchanger and then used as an oxygen source to enter the methane reformer's combustion chamber for combustion. The exhaust gas from the combustion chamber is then recycled by a waste heat recovery device. Simultaneously, CO2 is enriched in the exhaust gas and recovered by a CO2 capture device. The recovered CO2 can be used as a raw material for dimethyl carbonate or sold as experimental gas.
[0038] The oxygen in the air and the fuel undergo an electrochemical reaction at the anode and cathode of the solid oxide fuel cell, causing electron transfer to generate current. After passing through the DC / DC voltage regulator and inverter, the electrical energy is output and supplied to other electrical equipment.
[0039] A combustion chamber is provided inside the methane reforming reaction device to provide a heat source for the methane reforming reaction. The temperature required for the methane reforming reaction needs to be determined according to the specific catalyst and reaction process.
[0040] Composition of solid oxide fuel cell (SOFC): A typical SOFC core consists of three parts: cathode, anode and electrolyte. Due to the low output power of a single cell, in practical applications, in order to achieve sufficient output power, a series of single cells are usually connected into a battery stack using connectors and sealing materials.
[0041] The working principle of SOFC is as follows Figure 4 As shown in the figure, the electrolyte separates the anode and cathode, allowing the oxidation reaction and reduction reaction to take place in separate electrode spaces. The oxidant on the cathode side (O2 in the air) is reduced to oxygen ions (O 2- ) and then transported to the anode side through the oxygen ion conductor electrolyte. 2- Electrochemical reaction occurs with fuel (hydrogen, carbon monoxide, methane, etc.) on the anode side, and the electrons (e - ) is transmitted through an external circuit, generating an electric current. The reaction temperature ranges from 600°C to 1000°C, with the optimum temperature varying depending on the structural type. Currently, SOFC operating temperatures are trending towards lower temperatures. Commercial SOFCs often use metal-ceramic composite anode materials and operate between 650°C and 750°C.
[0042] Solid oxide fuel cell reaction equation:
[0043] Anode: CO+O 2- =CO2; H2+O 2- =H2O
[0044] Cathode: O2+4e - =2O 2-
[0045] Overall reaction: CO + H2 + O2 = CO2 + H2O
[0046] The methanol purge gas released from the methanol synthesis unit has a temperature of 41°C and a pressure of 74 bar. The ratio of recycle gas to methanol purge gas is approximately 100:1. Although the methanol purge gas accounts for only 1%, for a chemical plant with an annual methanol production of 600,000 tons, the flow rate of methanol purge gas is approximately 399.62 kmol / h (3818 kg / h). The hydrogen-rich gas flow rate after hydrogen recovery is 287 kmol / h (1267 kg / h), the tail gas flow rate is 112.62 kmol / h (2551 kg / h), and the gas temperature is approximately 40°C. The main component parameters of the relevant gases are as follows:
[0047] <![CDATA[N2(mol%)]]> CO (mol%) <![CDATA[CH4(mol%)]]> <![CDATA[CO2(mol%)]]> <![CDATA[H2(mol%)]]> 11.72 6.86 8.35 2.32 70.73
[0048] Table 1 Main components of typical methanol purge gas
[0049] <![CDATA[N2(mol%)]]> CO (mol%) <![CDATA[CH4(mol%)]]> <![CDATA[CO2(mol%)]]> <![CDATA[H2(mol%)]]> 2.5 2.1 0.53 1.65 91.99
[0050] Table 2 Main composition of hydrogen-rich gas after methanol purge gas hydrogen recovery
[0051] <![CDATA[N2(mol%)]]> CO (mol%) <![CDATA[CH4(mol%)]]> <![CDATA[CO2(mol%)]]> <![CDATA[H2(mol%)]]> 38.82 16.9 7.35 3.79 33.02
[0052] Table 3 Main components of tail gas after methanol purge gas hydrogen recovery
[0053] <![CDATA[N2(mol%)]]> CO (mol%) <![CDATA[CH4(mol%)]]> <![CDATA[CO2(mol%)]]> <![CDATA[H2(mol%)]]> 9.62 11.3 2.21 2.16 71.65
[0054] Table 4 Main components of methanol synthesis gas
[0055] 1. Calculation of power generation from tail gas after hydrogen recovery from methanol purge gas:
[0056] The exhaust gas flow rate is 112.62 kmol / h (2551 kg / h), so the volume flow rate is 112.62×22.4=2522.688 Nm 3 / h, the gases that can be used for power generation are CO, CH4, and H2.
[0057] Electric energy per unit volume of CO (kW·h / Nm 3 ) is 3.51;
[0058] Volume flow rate of CO (Nm 3 / h) is 2522.688×16.9×0.01≈426.33
[0059] 426.33Nm 3 The theoretical power generation capacity of CO2 / h is 426.33×3.51≈1496.42kW.
[0060] The electrical energy per unit volume of CH4 (kW·h / Nm 3 ) is 10;
[0061] Volume flow rate of CH4 (Nm 3 / h) is 2522.688×7.35×0.01≈185.42
[0062] 185.42Nm 3 The theoretical power generation of CH4 per hour is 185.42×10=1854.2kW
[0063] The electrical energy per unit volume of H2 (kW·h / Nm 3 ) is 3;
[0064] Volume flow rate of H2 (Nm 3 / h) is 2522.688×33.02×0.01≈832.99
[0065] 832.99Nm 3 The theoretical power generation of H2 / h is 832.99×3=2498.97kW
[0066] Therefore, the theoretical power generation capacity of methanol off-gas after hydrogen recovery for one hour is:
[0067] 1496.42+1854.2+2498.97kW=5849.59kW
[0068] If the SOFC fuel conversion rate is 60%, the power generation of the tail gas after methanol purge gas hydrogen recovery for one hour is: 5849.59×0.6=3509.754≈3510kW
[0069] 2. Carbon emission accounting of this plan:
[0070] The tail gas flow rate is 112.62 kmol / h (2551 kg / h). The carbon-containing substances are CO, CH4, and CO2. The total proportion (mol%) in the tail gas is: 16.9+7.35+3.79=28.04. Assuming that the carbon-containing substances are completely converted into CO2,
[0071] According to the material balance, the flow rate of CO2 in the flue gas after the reaction is 112.62×28.04×0.01≈31.58kmol / h, and the mass flow rate is 31.58×44=1389.52kg / h. 1389.52kg of CO2 needs to be captured per hour.
[0072] Based on a carbon capture efficiency of 90%, the amount of CO2 emissions that can be reduced per hour is:
[0073] 1389.52×0.9=1250.568≈1251kg.
[0074] In summary, the beneficial effects of this embodiment are as follows:
[0075] 1. Compared with traditional IGFC technology, this solution does not directly use high-value-added, high-concentration synthesis gas for power generation. Instead, it uses the tail gas recovered from methanol purge gas with hydrogen, which has a lower recovery value, to generate electricity. Taking a chemical plant with an annual methanol output of 600,000 tons as an example, the fuel contained in the tail gas after methanol purge gas hydrogen recovery can generate approximately 3510kW of power per hour, which is practical. In addition, the tail gas recovered from methanol purge gas with hydrogen does not require dust removal, desulfurization and other processes, and the process is simple and low-cost.
[0076] 2. Compared with the traditional tail gas treatment method - tail gas combustion for heat supply, the CO2 generated by this solution is very concentrated, easy to capture and utilize, which can significantly reduce carbon reduction costs and achieve near-zero carbon dioxide emissions. Taking a chemical plant with an annual production of 600,000 tons of methanol as an example, according to this solution, carbon dioxide emissions are reduced by approximately 1,251 kg per hour.
[0077] In the description of this application, it should be noted that, unless otherwise expressly specified or limited, the terms "mounted," "connected," and "connected" should be understood in a broad sense. For example, they may refer to fixed connections, detachable connections, or integrated connections; they may refer to mechanical connections or electrical connections; they may refer to direct connections or indirect connections through an intermediate medium; and they may refer to internal communication between two components. Those skilled in the art will understand the specific meanings of the above terms in this application in specific contexts.
[0078] If the present invention discloses or involves components or structural parts that are fixedly connected to each other, then, unless otherwise stated, the fixed connection can be understood as: a detachable fixed connection (for example, connection using bolts or screws), and can also be understood as: a non-detachable fixed connection (for example, riveting, welding). Of course, the mutual fixed connection can also be replaced by an integrated structure (for example, manufactured by integral molding using a casting process) (except where it is obviously impossible to use an integrated molding process).
[0079] In addition, unless otherwise stated, the terms used in any technical solution disclosed in the above-mentioned utility model to express positional relationships or shapes include states or shapes that are approximate, similar or close thereto.
[0080] Any component provided by the present invention may be assembled from a plurality of separate components, or may be a separate component manufactured by an integral forming process.
[0081] Adaptive changes based on actual needs are all within the protection scope of this utility model.
[0082] It should be noted that it is obvious to those skilled in the art that the present invention is not limited to the details of the exemplary embodiments described above, and that the present invention can be implemented in other specific forms without departing from the spirit or essential characteristics of the present invention. Therefore, from all perspectives, the embodiments should be regarded as illustrative and non-restrictive. The scope of the present invention is defined by the appended claims, not the foregoing description, and it is intended that all variations within the meaning and range of equivalents of the claims be encompassed within the present invention. Any reference signs in the claims should not be construed as limiting the claim to which they relate.
[0083] The present invention uses specific examples to illustrate the principles and implementation methods of the present invention. The above examples are only intended to help understand the method and core concept of the present invention. At the same time, those skilled in the art will find that the specific implementation methods and application scopes may vary based on the concept of the present invention. In summary, the contents of this specification should not be construed as limiting the present invention.
Claims
1. A methanol purge gas hydrogen recovery tail gas utilization system, characterized by: It includes a solid oxide fuel cell, a gas supply unit and an oxygen supply unit; The gas supply unit includes a methanol synthesis device, a hydrogen recovery device, a preheating device and a methane reforming reaction device which are connected in sequence; The methane reforming reaction device includes a reaction chamber for performing a reforming reaction and a combustion chamber for providing heat for the reforming reaction, wherein the outlet of the reaction chamber is connected to the anode inlet of the solid oxide fuel cell, the anode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber, and the outlet of the combustion chamber is connected to a CO2 capture device; The oxygen supply unit includes an oxygen supply source and a heat exchange device connected in sequence, the cold side outlet of the heat exchange device is connected to the cathode inlet of the solid oxide fuel cell, and the cathode outlet of the solid oxide fuel cell is connected to the inlet of the combustion chamber.
2. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 1, characterized in that: The outlet of the hydrogen recovery device is communicated with the inlet of the combustion chamber.
3. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 1, characterized in that: The outlet of the oxygen supply source is communicated with the inlet of the combustion chamber.
4. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 3, characterized in that: The oxygen supply source is an air compressor or a blower.
5. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 1, characterized in that: The cathode outlet of the solid oxide fuel cell is communicated with the hot side inlet of the heat exchange device, and the hot side outlet of the heat exchange device is communicated with the inlet of the combustion chamber.
6. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 1, characterized in that: A waste heat recovery device is provided between the combustion chamber and the CO2 capture device.
7. The methanol purge gas hydrogen recovery tail gas utilization system according to claim 6, characterized in that: The waste heat recovery device is communicated with the preheating device.