Device suitable for preparing methanol from diversified feed gas

Abstract

The utility model discloses a device suitable for preparing methanol from diversified feed gas. The device comprises a hydrogen pressurization system, a compression system, a reaction system and a separation system, the hydrogen pressurizing system automatically controls the amount of the added hydrogen according to the component change condition of the gas sent by the previous working section, so that the hydrogen-carbon ratio of the gas entering the synthesis working section is adjusted in time; the compression system compresses the raw material gas and sends out the pressurized raw material gas through the pressurized raw material gas outlet into the reaction system for reaction; and the separation system receives the reaction gas output by the reaction system, separates crude methanol and sends out the crude methanol from a crude methanol outlet. According to the utility model, the process flow of the whole plant is simplified by optimizing the traditional methanol synthesis process, the investment cost of the device is reduced, meanwhile, the device is adaptive to various different feed gas process flows, and the influence of fluctuation generated by a single unstable gas source on the methanol production process is reduced. According to the method, tail gas and heat generated in methanol production can be recycled, and resource waste is reduced.

Description

Technical Field

[0001] The utility model relates to the field of methanol synthesis, and particularly relates to a methanol production device suitable for preparing methanol with diversified raw material gases. Background Technique

[0002] Methanol is one of the most basic organic chemical raw materials. Its industrial chain is long and it is widely used in many industries such as chemical industry, building materials, energy, medicine, pesticides, etc., playing a supporting role in the development of the national economy. In the traditional chemical industry, methanol is the upstream raw material of many chemical products, such as formaldehyde, dimethyl ether, acetic acid, etc., and these products play an indispensable role in the chemical industry.

[0003] In the process of methanol synthesis, the hydrogen-carbon ratio of the raw material gas has an important impact on the reaction efficiency and product quality. If the hydrogen-carbon ratio is too low, side reactions will increase, the decline of catalyst activity will be accelerated, and carbon deposition reactions may also be caused; while if the hydrogen-carbon ratio is too high, hydrogen accumulation will occur, the content of inert gases will increase, and thus the consumption will increase. In the catalytic reaction of methanol synthesis, maintaining an appropriate hydrogen-carbon ratio is crucial, which directly affects the yield and quality of methanol. However, due to the complex raw material gas preparation process, gas component fluctuations, and harsh reaction conditions, real-time monitoring and precise adjustment of the hydrogen-carbon ratio are a long-term technical challenge.

[0004] In order to ensure the stability of the raw material gas, complex equipment and delicate operations are required to adjust and control the reaction conditions, which increases the complexity of the production process and the operation difficulty. The current mainstream technology is to regulate the hydrogen-carbon ratio of the raw material gas through methods such as carbon monoxide conversion and carbon dioxide removal, and form a raw material gas with stable components and send it to the methanol synthesis section. However, whether it is coal, natural gas, industrial waste gas, or biomass, it will inevitably cause the instability of the components of the produced raw material gas. At the same time, the increase in equipment and processes will also increase the production cost.

[0005] In addition, the traditional production methods of methanol face problems such as large energy consumption and low raw material utilization efficiency. These processes usually involve a large amount of energy input, resulting in an unsatisfactory overall energy efficiency. And due to the limitations of reaction conditions and insufficient process control, the raw materials are often not fully utilized during the conversion process, thus causing significant waste of resources. This inefficient use of resources not only increases the production cost but also imposes an unnecessary burden on the environment.

[0006] In the industrial process of methanol production, the stability of the feed gas supply is crucial. However, this stability is affected by various factors, including the production method of the feed gas, fluctuations in market demand, and other supply chain issues. These external factors may cause fluctuations in the composition and pressure of the feed gas, which pose challenges to maintaining the continuity and efficiency of the methanol production process. Unstable feed gas composition may affect the balance of chemical reactions, reducing the yield and quality of the product, while pressure fluctuations may lead to abnormal equipment operation and even potential safety hazards. Therefore, it is required that the production facilities must have a high degree of adaptability and flexibility, be able to monitor and adjust operating parameters in real time to adapt to changes in the feed gas supply, and ensure the stability and safety of the production process. In addition, adopting flexible production strategies and establishing a diversified gas source supply chain can, to a certain extent, reduce the dependence on a single supply source, thereby enhancing the enterprise's ability to respond to market and environmental changes. By implementing these strategies and technologies, methanol production enterprises can not only improve production efficiency and product quality but also ensure the long-term sustainable development and market competitiveness of the enterprise. Summary of the Utility Model

[0007] In view of the key challenges faced in current methanol production, the present utility model aims to provide a methanol production device suitable for diversified feed gas preparation. This device can precisely control the hydrogen-carbon ratio through precise control and automatic hydrogen addition. This device can not only adapt to a variety of different feed gases but also reduce the impact of fluctuations caused by a single unstable gas source on the methanol production process.

[0008] The technical problems to be solved by the present utility model can be achieved through the following technical solutions:

[0009] A methanol production device suitable for diversified feed gas preparation, comprising:

[0010] A hydrogen pressurization system, which automatically controls the amount of hydrogen added according to the change in the gas composition sent from the previous section, thereby timely adjusting the hydrogen-carbon ratio of the gas entering the synthesis section; the hydrogen pressurization system has a pressurized hydrogen output port and a hydrogen inlet,

[0011] A compression system, which has a first feed gas input port and a pressurized feed gas output port, the pressurized hydrogen output port is connected to the first feed gas input port or the pressurized hydrogen output port is connected to the pressurized feed gas output port, and the compression system compresses the feed gas and sends it out through the pressurized feed gas output port;

[0012] A reaction system, which has a pressurized feed gas inlet and a reaction gas outlet; the pressurized feed gas output port is connected to the pressurized feed gas inlet, and the pressurized feed gas output by the compression system enters the reaction system for reaction;

[0013] A separation system, the separation system having a reaction gas inlet and a crude methanol outlet, the reaction gas inlet being connected to the reaction gas outlet, receiving the reaction gas output from the reaction system and separating the crude methanol and sending it out from the crude methanol outlet.

[0014] In a preferred embodiment of the present utility model, the separation system further has a first purge gas outlet and the methanol production device applicable to diversified raw material gases further includes a hydrogen recovery system and a methane recovery system. The hydrogen recovery system has a first purge gas inlet, a recovered hydrogen outlet and a gas outlet after hydrogen recovery. The methane recovery system has a gas inlet after hydrogen recovery and a green LNG outlet. The first purge gas inlet is connected to the first purge gas outlet, the recovered hydrogen outlet is connected to the first hydrogen output port, the gas inlet after hydrogen recovery is connected to the gas outlet after hydrogen recovery, and the green LNG outlet sends out green LNG to the outside of the plant.

[0015] A methanol production device applicable to diversified raw material gases, comprising:

[0016] A hydrogen recovery system, the hydrogen recovery system having a second raw material gas input port, a second purge gas inlet, a recovered hydrogen outlet and a gas outlet after hydrogen recovery;

[0017] A compression system, the compression system having a first raw material gas input port, a pressurized raw material gas outlet and a superheated steam inlet, the recovered hydrogen outlet being connected to the first raw material gas input port, and the compression system compressing the raw material gas and sending it out through the pressurized raw material gas outlet;

[0018] A reaction system, the reaction system having a pressurized raw material gas inlet, a reaction gas outlet and a steam outlet; the pressurized raw material gas outlet is connected to the pressurized raw material gas inlet, the pressurized raw material gas output by the compression system enters the reaction system for reaction, the reacted reaction gas is sent out from the reaction gas outlet, and the steam takes away the heat of the reaction system and is sent out from the steam outlet;

[0019] A separation system, the separation system having a reaction gas inlet, a crude methanol outlet and a second purge gas outlet, the reaction gas inlet being connected to the reaction gas outlet, receiving the reaction gas output from the reaction system and separating the crude methanol and sending it out from the crude methanol outlet, and the second purge gas outlet being connected to the second purge gas inlet;

[0020] A steam superheating system, the steam superheating system having a steam inlet, a gas inlet after hydrogen recovery, a superheated steam outlet, the steam inlet being connected to the steam outlet, the gas inlet after hydrogen recovery being connected to the gas outlet after hydrogen recovery, and the superheated steam outlet being connected to the superheated steam inlet.

[0021] Due to the adoption of the above technical solution, the utility model simplifies the whole plant process flow and reduces the device investment cost by optimizing the traditional methanol synthesis process. This method can recycle the tail gas and heat generated in methanol production, reducing resource waste.

[0022] The specific achievable effects are as follows:

[0023] 1. The utility model is provided with a hydrogen pressurization system, which automatically controls the amount of hydrogen added according to the change of gas components sent from the previous section, so as to timely adjust the hydrogen-carbon ratio of the gas entering the synthesis section. It has a high degree of automation and a fast device adjustment feedback speed, and is especially suitable for production devices with a large fluctuation in gas source components.

[0024] 2. The hydrogen pressurization system involved in the utility model determines the amount of hydrogen to be added by setting relevant gas flow and component analysis instruments, sending the composition and relevant flow rates of CO, CO2 and H2 in the raw material gas to the calculation module, and then comparing and analyzing with the empirical set value (M=(H2-CO2) / (CO+CO2)), so as to finally achieve precise control of the hydrogen-carbon ratio.

[0025] 3. The hydrogen addition method involved in the utility model can adapt to raw material gases with different pressures. A separate compression system can be configured, and the appropriate hydrogen addition position can be determined according to the on-site layout, with high hydrogen addition flexibility; or a combined compression system can be set up, that is, sharing a set of units with the fresh gas, reducing the investment cost.

[0026] 4. The utility model is provided with a steam superheat system, which uses the purge gas from methanol synthesis as fuel gas to by-product superheated steam, realizing the recycling of waste gas. At the same time, the by-product superheated steam can be used as power steam to drive the turbine of the compression system, achieving the purpose of energy conservation. It is especially suitable for production devices with a relatively high inert gas content, where the purge gas volume in the methanol synthesis section is large, and the energy-saving effect of the device is obvious.

[0027] 5. The utility model is provided with a methane recovery system, which is especially suitable for production devices with a relatively high methane content. The purge gas from methanol synthesis can be sent to the LNG liquefaction cold box to realize the co-production of methanol and LNG products, achieving the comprehensive utilization of resources.

[0028] 6. The utility model relates to hydrogen recovery from part of the raw material gas, which is applicable to a production device with a relatively low hydrogen-carbon ratio in the raw material gas components and no external hydrogen supply source. By directly sending part of the raw material gas to the hydrogen recovery system and returning the extracted hydrogen-rich gas to the methanol synthesis loop, the hydrogen-carbon ratio required for methanol synthesis can be achieved. The hydrogen recovery system can adopt means such as pressure swing adsorption or membrane separation. Since a methanol synthesis device usually has a purge gas hydrogen recovery system, the hydrogen recovery scale involved in the utility model will increase, but the conventional raw material gas conversion and decarbonization treatment processes can be omitted, greatly simplifying the whole plant process flow and device investment cost.

[0029] 7. The utility model is provided with a reaction system temperature control module. When the gas component changes sent from the previous section or the upstream supply of the supplementary hydrogen source fluctuates, it automatically adjusts the steam drum pressure of the reaction system, and then adjusts the reaction system bed temperature, so as to maintain the methanol synthesis reaction to the greatest extent and achieve the flexible and stable production of the methanol device. It is especially applicable to a green methanol device, and the supply of its supplementary hydrogen source is easily affected by upstream renewable resources such as wind and light.

[0030] 8. The reaction system temperature control module involved in the utility model sends information such as the flow rates and components of the raw material gas, the gas entering the tower, and the recycle gas to the calculation module by setting relevant gas flow rate and component analysis instruments, and then determines the most suitable reaction temperature value through comparison and analysis with the empirical set value, finally realizing the dynamic adjustment of the device. BRIEF DESCRIPTION OF THE DRAWINGS

[0031] Figure 1 It is a schematic flow chart of the device for preparing green methanol and co-producing green LNG with biomass gasification coupled with green hydrogen as the raw material gas in Embodiment 1 of the utility model.

[0032] Figure 2 It is a schematic flow chart of the device for preparing methanol with natural gas non-catalytic partial oxidation conversion gas as the raw material in Embodiment 2 of the utility model. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0033] The following further describes the utility model in conjunction with the drawings and specific embodiments.

[0034] Embodiment 1

[0035] See Figure 1, a methanol production device suitable for diversified raw material gas shown in the figure is a device for producing green methanol and co-producing green LNG with biomass gasification coupled with green hydrogen as the raw material gas, including a hydrogen pressurization system (hydrogen control module) 100, a compression system 200, a reaction system (temperature control module) 300, a hydrogen recovery system 400, a methane recovery system 500, and a separation system 600. The hydrogen pressurization system 100 automatically controls the amount of hydrogen injected according to the change of gas components sent from the previous section, so as to timely adjust the hydrogen-carbon ratio of the gas entering the synthesis section; the hydrogen pressurization system 100 has a hydrogen inlet 110 and a pressurized hydrogen outlet 120.

[0036] The compression system 200 has a first raw material gas inlet 210 and a pressurized raw material gas outlet 220. The pressurized hydrogen outlet 120 is connected to the pressurized raw material gas outlet 220. At this time, the compression system 200 compresses the raw material gas and sends it out through the pressurized raw material gas outlet 220. Or the pressurized hydrogen outlet 120 is connected to the raw material gas inlet 210. At this time, the compression system 200 compresses the hydrogen and the raw material gas and sends it out through the pressurized raw material gas outlet 220.

[0037] The reaction system 300 has a pressurized raw material gas inlet 310 and a reaction gas outlet 320; the pressurized raw material gas outlet 220 is connected to the pressurized raw material gas inlet 310, and the pressurized raw material gas output by the compression system 200 enters the reaction system 300 for reaction.

[0038] The separation system 600 has a reaction gas inlet 610, a crude methanol outlet 620, and a first purge gas outlet 630. The reaction gas inlet 610 is connected to the reaction gas outlet 320, receives the reaction gas output by the reaction system 300, and separates the crude methanol and sends it out through the crude methanol outlet 620.

[0039] The hydrogen recovery system 400 has a first purge gas inlet 410, a recovered hydrogen outlet 420, and a gas outlet 430 after hydrogen recovery. The methane recovery system 500 has a gas inlet 510 after hydrogen recovery and a green LNG outlet 520. The first purge gas inlet 410 is connected to the first purge gas outlet 630, the recovered hydrogen outlet 420 is connected to the first hydrogen output port 110, the gas inlet 510 after hydrogen recovery is connected to the gas outlet 430 after hydrogen recovery, and the green LNG outlet sends out green LNG to the outside of the plant.

[0040] The working principle of this embodiment is as follows:

[0041] The hydrogen inlet 110 of the hydrogen pressurization system 100 receives green hydrogen 1. The pressurized hydrogen 2 passes through the pressurized hydrogen outlet 120. According to factors such as the pressure of the raw material gas 3 and the site layout in the actual production process, the hydrogen addition position can be preferably selected before or after the compression system 200, that is, the pressurized hydrogen outlet 120 is connected to the raw material gas inlet 210 or the pressurized hydrogen outlet 120 is connected to the pressurized raw material gas outlet 220.

[0042] If the pressure of the pressurized hydrogen 2 cannot directly enter the reaction system, hydrogen addition before the compression system 200 is selected for secondary pressurization. If the pressure of the pressurized hydrogen 2 can directly enter the reaction system, the method of hydrogen addition after the compression system 200 is selected.

[0043] The green raw material gas 0 is mixed with the recycled hydrogen 9 sent out from the recycled hydrogen outlet 420 of the hydrogen recovery system 400 to form the raw material gas 3.

[0044] When hydrogen addition before the compression system 200 is preferably selected, the green raw material gas 3 is first mixed with the pressurized hydrogen 2.1 to form the raw material gas 4, and then enters the compression system 200. The pressurized raw material gas 5 after pressurization is sent to the reaction system (temperature control module) 300 through the pressurized raw material gas outlet 220. When hydrogen addition after the compression system 200 is preferably selected, the compression system 200 receives the green raw material gas 3 for pressurization, and after pressurized hydrogen addition, the pressurized raw material gas 5 and the pressurized hydrogen 2.2 are sent to the reaction system 300 together.

[0045] In this example, the pressure of the green raw material gas 3 is about 3 MPa, the pressure of the green hydrogen 1 is about 1.5 MPa, and hydrogen addition before the compression system 200 is preferably selected. The pressure of the pressurized hydrogen is about 3.1 - 3.3 MPa. The hydrogen pressurization system 100 only needs to select one-stage compression, reducing the investment in hydrogen compressors. The flow rate of the green raw material gas 3 is about 56000 Nm 3 / h. Its components (mole fraction percentage) are roughly as follows:

[0046] CO: 32% - 38%

[0047] CO2: 3% - 8%

[0048] H2: 50% - 55%

[0049] CH4: 5% - 10%

[0050] The hydrogen control module is included in the hydrogen pressurization system 100. The function of this module is to automatically control the amount of hydrogen added (about 16000 Nm 3 / h) according to the immediate components of the green raw material gas 3 and the set value of the empirical hydrogen-carbon ratio (M = 2.05 - 2.15).

[0051] The reaction system 300 receives the raw material gas 5 with a stable hydrogen-carbon ratio for methanol synthesis reaction. The reaction system in this embodiment is about 5 MPa. A temperature control module is set in the system. The appropriate reaction temperature (230 - 260 °C), steam drum pressure (2.5 - 4.0 MPa) and other process parameters can be determined according to the flow rate, components and other relevant physical property data of the green raw material gas and the empirical set values.

[0052] At the same time, the temperature control module and the hydrogen control module are linked and regulated, which can solve the problems of reactor temperature loss, runaway temperature and even plant shutdown caused by the sudden fluctuations in the sources of "green hydrogen" and "green carbon" under abnormal conditions. It enables the entire green methanol synthesis system to achieve integrated dynamic regulation.

[0053] The separation system 600 receives the reaction gas 6 after the reaction, and sends the liquid-phase crude methanol 7 to the next section for in-depth treatment through the crude methanol outlet 620 after operations such as separation, filtration, and flash evaporation. The gas-phase components enter the hydrogen recovery system 400 as the purge gas 8 from the first purge gas outlet 630.

[0054] The hydrogen recovery system 400 receives about 15000 Nm 3 / h of the purge gas 8. The recovered hydrogen 9 sent out through the recovered hydrogen outlet 420 has a pressure of 3.1 MPa and a flow rate of about 10000 Nm 3 / h. It is mixed into the green raw material gas 0 and continues to participate in the methanol synthesis reaction. The gas 10 after hydrogen recovery sent out through the gas outlet 430 after hydrogen recovery is about 5000 Nm 3 / h. Its components are mostly inert gases (such as CH4, N2, etc., about 70%) that do not participate in the methanol synthesis, as well as a small amount of unreacted carbon (CO + CO2: about 10%) and hydrogen (H2: about 20%). The content of methane (>50%) is quite considerable.

[0055] The gas 10 after hydrogen recovery sent out through the gas outlet 430 after hydrogen recovery is sent into the methane recovery system 500, and after recovery, the green LNG 11 is separated out as a by-product through the LNG liquefaction cold box.

[0056] Example 2

[0057] See Figure 2 , a methanol production device suitable for diversified raw material gases shown in the figure is a device for producing methanol using the non-catalytic partial oxidation conversion gas of natural gas as the raw material, including a compression system 200, a reaction system 300, a hydrogen recovery system 700, a steam superheating system 800, and a separation system 600.

[0058] The hydrogen recovery system 700 has a second raw material gas input port 710, a second purge gas inlet 720, a recovered hydrogen outlet 730, and a gas outlet 740 after hydrogen recovery;

[0059] The compression system 200 has a first raw gas inlet 210, a pressurized raw gas outlet 220, and a superheated steam inlet 230. The recovered hydrogen outlet 730 is connected to the first raw gas inlet 210. The compression system 200 compresses the raw gas and sends it out through the pressurized raw gas outlet 220.

[0060] The reaction system 300 has a pressurized raw gas inlet 310, a reaction gas outlet 330, and a steam outlet 320. The pressurized raw gas outlet 220 is connected to the pressurized raw gas inlet 310. The pressurized raw gas output by the compression system 200 enters the reaction system 300 for reaction. The reacted reaction gas is sent out through the reaction gas outlet 330, and the steam takes away the heat of the reaction system and is sent out through the steam outlet 320.

[0061] The separation system 600 has a reaction gas inlet 610, a crude methanol outlet 620, and a second purge gas outlet 640. The reaction gas inlet 610 is connected to the reaction gas outlet 330, receives the reaction gas output by the reaction system 300, separates the crude methanol, and sends it out through the crude methanol outlet 620. The second purge gas outlet 640 is connected to the second purge gas inlet 720.

[0062] The steam superheating system 800 has a steam inlet 810, a gas inlet 820 after hydrogen recovery, and a superheated steam outlet 830. The steam inlet 810 is connected to the steam outlet 330. The gas inlet 820 after hydrogen recovery is connected to the gas outlet 740 after hydrogen recovery. The superheated steam outlet 830 is connected to the superheated steam inlet 230.

[0063] The raw gas 12 is divided into two streams. One stream of the raw gas 13 enters the hydrogen recovery system 700 through the second raw gas inlet 710 of the hydrogen recovery system 700. The other stream of the raw gas 14 is mixed with the hydrogen 15 (about 80,000 Nm 3 / h) sent out from the recovered hydrogen outlet 730 of the hydrogen recovery system 700 to form the raw gas 15, which is sent into the compression system 200 and pressurized to 8 MPa. The pressurized raw gas 4 enters the reaction system 300.

[0064] The flow rate of the raw gas 12 is about 350,000 Nm 3 / h, and the pressure is 5.0 MPa. The raw gas prepared by the non-catalytic partial oxidation conversion of natural gas has a relatively low hydrogen-carbon ratio, which is 1.5 - 1.8. Its components (mole percentage) are roughly as follows:

[0065] CO: 35% - 40%

[0066] CO2: 3% - 5%

[0067] H2: 60% - 65%

[0068] CH4: 0.5% - 1%

[0069] The hydrogen recovery system 700 (hydrogen control module) receives two gas streams, namely the feed gas 13 and the purge gas 16 from the separation system 600. That is, a part of the feed gas and the synthesis purge gas are sent together to the hydrogen recovery system 700 for hydrogen extraction, thus eliminating the conventional feed gas conversion and decarbonization processes, and greatly simplifying the whole plant process flow and equipment investment cost.

[0070] The hydrogen recovery system 700 is internally provided with a hydrogen control module. According to the purge gas 16, the feed gas 13, and the empirical hydrogen-carbon ratio set value (M = 2.05 - 2.15), it analyzes, calculates, and controls the feed gas 13 input amount and the hydrogen 15 supplement amount. Under the adjustment of the hydrogen control module, the hydrogen-carbon ratio of the pressurized feed gas 17 entering the reaction system 300 is kept stable. At the same time, the hydrogen in the purge gas 16 can also be reused.

[0071] After receiving the stable pressurized feed gas 17, the reaction system 300 conducts methanol synthesis reaction, and the water circulation in the steam drum takes away the steam generated by the reaction. There are two outlets from the reaction system 300, namely the crude methanol 18 sent to the separation system 600, and the 250 °C steam 19 produced by the steam drum sent to the steam superheating system 800.

[0072] The separation system 600 receives the reacted material 18, and through operations such as separation, filtration, and flash evaporation, the liquid-phase crude methanol 21 is sent to the next section for in-depth treatment. The gas-phase component 16 is about 50000 Nm 3 / h enters the hydrogen recovery system as the purge gas.

[0073] The purge gas 23 after hydrogen recovery by the hydrogen recovery system is rich in a large amount of combustible gases such as CH4, CO, CO2, and H2. The purge gas 23 is sent to the steam superheating system as fuel gas to provide heat for the steam superheating system, and the steam 19 is turned into superheated steam 24. The produced superheated steam is transported to the compression system and can be used to drive the compressor turbine of the compression system 200, saving energy loss. This process flow has obvious energy-saving effects for production devices with a high inert gas content in the gas source.

Claims

1. An apparatus suitable for preparing methanol from diversified raw material gases, characterized in that, Comprising: A hydrogen pressurization system, which automatically controls the amount of hydrogen fed in according to the change of gas components sent from the previous section, so as to timely adjust the hydrogen-carbon ratio of the gas entering the synthesis section; the hydrogen pressurization system has a pressurized hydrogen output port and a hydrogen inlet, A compression system, which has a first raw material gas input port and a pressurized raw material gas output port, the pressurized hydrogen output port is connected to the first raw material gas input port or the pressurized hydrogen output port is connected to the pressurized raw material gas output port, and the compression system compresses the raw material gas and sends it out through the pressurized raw material gas output port; A reaction system, which has a pressurized raw material gas inlet and a reaction gas outlet; the pressurized raw material gas output port is connected to the pressurized raw material gas inlet, and the pressurized raw material gas output by the compression system enters the reaction system for reaction; A separation system, which has a reaction gas inlet and a crude methanol outlet, the reaction gas inlet is connected to the reaction gas outlet, receives the reaction gas output by the reaction system and separates the crude methanol and sends it out from the crude methanol outlet.

2. The device for preparing methanol from diversified raw material gas according to claim 1, characterized in that, The separation system also has a first purge gas outlet and the methanol production device suitable for diversified raw material gases further includes a hydrogen recovery system and a methane recovery system. The hydrogen recovery system has a first purge gas inlet, a recovered hydrogen outlet and a gas outlet after hydrogen recovery. The methane recovery system has a gas inlet after hydrogen recovery and a green LNG outlet. The first purge gas inlet is connected to the first purge gas outlet, the recovered hydrogen outlet is connected to the first hydrogen output port, the gas inlet after hydrogen recovery is connected to the gas outlet after hydrogen recovery, and the green LNG outlet sends out green LNG to the outside of the plant.

3. An apparatus for preparing methanol from diversified raw material gases, characterized in that, Comprising: A hydrogen recovery system, which has a second raw material gas input port, a second purge gas inlet, a recovered hydrogen outlet and a gas outlet after hydrogen recovery; A compression system, which has a first raw material gas input port, a pressurized raw material gas output port and a superheated steam inlet, the recovered hydrogen outlet is connected to the first raw material gas input port, and the compression system compresses the raw material gas and sends it out through the pressurized raw material gas output port; A reaction system, which has a pressurized raw material gas inlet, a reaction gas outlet and a steam outlet; the pressurized raw material gas output port is connected to the pressurized raw material gas inlet, the pressurized raw material gas output by the compression system enters the reaction system for reaction, the reacted reaction gas is sent out from the reaction gas outlet, and the steam takes away the heat of the reaction system and is sent out from the steam outlet; A separation system, which has a reaction gas inlet, a crude methanol outlet and a second purge gas outlet, the reaction gas inlet is connected to the reaction gas outlet, receives the reaction gas output by the reaction system and separates the crude methanol and sends it out from the crude methanol outlet, and the second purge gas outlet is connected to the second purge gas inlet; A steam superheating system, the steam superheating system having a steam inlet, a gas inlet after hydrogen recovery, and a superheated steam outlet, the steam inlet being connected to the steam outlet, the gas inlet after hydrogen recovery being connected to the gas outlet after hydrogen recovery, and the superheated steam outlet being connected to the superheated steam inlet.

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