Methanol steam reforming hydrogen production process coupled with nuclear reactor

Abstract

The invention relates to the technical field of nuclear energy hydrogen production, and discloses a methanol steam reforming hydrogen production process of a coupled nuclear reactor, which combines a light water reactor unit with a reforming hydrogen production unit. And the light water reactor unit is used for providing a water vapor raw material and optional electric energy for the reforming hydrogen production unit. The light water nuclear reactor and methanol steam reforming hydrogen production are combined, the comprehensive utilization capacity of nuclear energy can be effectively improved, and the economical efficiency of the nuclear reactor is improved.

Description

Technical Field

[0001] The invention relates to the technical field of nuclear energy hydrogen production, and in particular to a methanol steam reforming hydrogen production process coupled with a nuclear reactor. Background Art

[0002] Nuclear energy, as a clean energy with high energy density, has good development prospects. Light water nuclear reactors are currently the world's main commercial nuclear reactor type, accounting for about 85% or more of the total number of nuclear reactors. Existing nuclear reactors are mainly used for power generation, but electricity is not easy to store, and the comprehensive utilization capacity and economy are poor. Hydrogen, as a clean secondary energy source, has high calorific value and is pollution-free. It can be widely used in industrial production. Electrolysis of water to produce hydrogen is one of the traditional methods of hydrogen production.

[0003] The current nuclear energy hydrogen production methods mainly include methane steam reforming hydrogen production, iodine-sulfur cycle thermochemical hydrogen production and high-temperature solid oxide electrolysis hydrogen production technology, but these hydrogen production technologies all require high-temperature heat supply above 700°C.

[0004] Chinese patent application No. 202110681565.0 discloses an efficient nuclear energy comprehensive utilization system that can realize flexible peak regulation of nuclear power plants, including a helium steam combined power generation system, a high-temperature solid oxide water electrolysis hydrogen production system and a seawater desalination system. The high-temperature and high-pressure helium generated by the high-temperature gas-cooled reactor completes power generation through the Brayton cycle. The low-pressure helium discharged from the helium turbine is used as a heat source to heat the feed water in the steam Rankine cycle and input into the steam turbine to complete power generation. The steam turbine outputs part of the steam, which enters the high-temperature solid oxide electrolysis hydrogen production system after the steam ejector adjusts the pressure and the high-temperature helium is heated to produce hydrogen, oxygen and water vapor through electrolysis, and is input into the seawater desalination system for desalination and heat recovery, realizing the coupling of power generation, hydrogen production and seawater desalination. When the high-temperature gas-cooled reactor of this system is combined with the high-temperature solid oxide water vapor electrolysis, the temperature of the intermediate heat exchanger reaches 950°C and the structure of the outlet header is complex. The high-temperature creep performance of the material is easy to change, resulting in a decrease in long-term load-bearing capacity and affecting the safety of the equipment. In addition, the raw water vapor for hydrogen production by electrolysis comes from steam turbines and pipeline extraction, so the steam cycle feed water needs to be continuously replenished.

[0005] It can be seen that the existing nuclear energy hydrogen production processes are mostly carried out under high temperature conditions, and require a continuous supply of additional circulating water, resulting in technical problems such as low conversion efficiency and high energy consumption. Summary of the invention

[0006] The present invention solves the technical problems of low methanol conversion efficiency and high energy consumption in the prior art, and provides a methanol steam reforming hydrogen production process coupled with a nuclear reactor, which effectively combines a light water nuclear reactor with methanol steam reforming hydrogen production. The light water reactor and methanol steam reforming hydrogen production in the present application can improve the methanol conversion efficiency, reduce energy consumption, and effectively improve the comprehensive utilization capacity of nuclear energy and the economic efficiency of nuclear reactors.

[0007] The object of the present invention is to provide a methanol steam reforming hydrogen production process coupled with a nuclear reactor, in which a light water reactor unit is used in conjunction with a reforming hydrogen production unit; the light water reactor unit provides steam raw materials and optional electrical energy for the reforming hydrogen production unit.

[0008] At present, high-temperature nuclear reactors are used to produce hydrogen in the field of nuclear energy hydrogen production, rather than low-temperature nuclear reactors. In the methanol steam reforming hydrogen production process of the present application, a light water nuclear reactor provides steam raw materials for the reforming hydrogen production unit. The inventors of the present application adjust the outlet steam temperature of the light water reactor to 220-300°C, use steam as the raw material for methanol reforming hydrogen production, and match the reforming temperature of methanol reforming hydrogen production. It is very convenient to adjust the mixing ratio and reaction temperature. On the one hand, the reasonable configuration and utilization of water vapor can be achieved to reduce energy consumption. On the other hand, the outlet steam temperature of the light water nuclear reactor is much lower than the outlet steam temperature of the existing nuclear energy hydrogen production reactor. The light water nuclear reactor does not need to be overly precisely controlled to achieve the reforming temperature within the appropriate temperature, and the methanol conversion rate of reforming hydrogen production is high, which can effectively improve the heat exchange efficiency and hydrogen yield.

[0009] According to a preferred embodiment of the present invention, the reforming hydrogen production unit includes a premixer I, a gasifier, a reformer, a gas-liquid separator and a purifier; the process includes the following steps:

[0010] S110, mixing a water vapor raw material from a light water reactor unit and a methanol raw material in a premixer I to obtain a mixed raw material A;

[0011] S120, sending the mixed raw material A into a gasifier for gasification, and then into a reformer for reforming to obtain a mixed gas B containing hydrogen and carbon dioxide;

[0012] S130, sending the mixed gas B to a gas-liquid separator for treatment to obtain a mixed gas C, and the mixed gas C is purified by a purifier to obtain hydrogen.

[0013] Preferably, a flow meter, a flow control valve and / or a pneumatic switch valve are connected to the connecting pipelines between the reactors as required.

[0014] According to a preferred embodiment of the present invention, the reforming conditions in step S120 include: a reforming temperature of 200-350°C, preferably 240-280°C, and more preferably 240-255°C; a reforming pressure of 5-15 bar, preferably 10-12 bar; and a water-to-alcohol mass ratio of (0.6-0.8):1, preferably (0.6-0.7):1.

[0015] In the methanol steam reforming reaction, SCST-401-53 catalyst is used, the main components of which are Cu-Zn-Al 2 O 3 -auxiliary agent, when studying the effect of temperature and pressure on the mass ratio of hydrogen in the product (the proportion of the total product gas), it was found that Figure 1 As shown, the reforming temperature remains unchanged, the lower the pressure, the higher the hydrogen mass ratio, that is, the higher the methanol conversion rate, and the heat load continues to decrease. When the reforming pressure remains unchanged, the temperature is 240-280℃, and the pressure starts from 11bar, the ratio of methanol to hydrogen turns to a slow decline, that is, at 250±10℃ and 11±1bar, the hydrogen production efficiency is the highest and the methanol conversion rate is the highest.

[0016] During methanol steam reforming, when studying the effect of temperature and pressure on the mass ratio of byproduct carbon monoxide (the ratio of the total product gas), it was found that the mass ratio of carbon monoxide tends to decrease with increasing pressure, and when the temperature increases, the mass ratio of carbon monoxide also increases step by step, which is proportional to the temperature. Figure 2 As shown, from the analysis of the change in the mass ratio of hydrogen in the upper part, it can be concluded that the hydrogen production rate is most suitable in the working range of 250±10℃, 11±1bar. A comprehensive analysis of the hydrogen mass ratio and the carbon monoxide mass ratio shows that the reforming working pressure and temperature range is 240℃-250℃, and the pressure is 11±1bar.

[0017] The inventors found that when the reforming pressure is fixed at 11 bar, at different temperatures, the higher the water-to-carbon ratio, the higher the hydrogen production, that is, the higher the methanol conversion rate. Figure 3 As shown, the effect of water-to-methanol ratio on hydrogen production at different temperatures. As the water-to-carbon molar ratio increases, the hydrogen production increases rapidly, and when the water-to-methanol molar ratio is 1.15 ± 0.05, the rate of increase decreases. Therefore, the present application selects a molar ratio of water to methanol of 1.15, that is, a water-to-methanol ratio of 0.627 as the optimal value. The water-to-carbon ratio is the molar ratio of raw water to methanol, and the water-to-methanol ratio is the mass ratio of raw water to methanol raw material.

[0018] According to a preferred embodiment of the present invention, in step S120, the temperature of the mixed raw material A when it is fed into the gasifier is 150-180°C, preferably 150-160°C.

[0019] According to a preferred embodiment of the present invention, the temperature of the methanol raw material entering the premixer I in step S110 is 25-35°C, and the pressure is 0.5-1.5 bar; the temperature of the water vapor raw material is 240-260°C, and the pressure is 20-25 bar; the mass flow ratio of the water vapor raw material to the methanol raw material is (0.6-0.7):1.

[0020] According to a preferred embodiment of the present invention, the reforming hydrogen production unit further includes a residual tail gas treatment system; preferably, the residual tail gas treatment system includes a premixer II, a combustion chamber and a tail gas processor;

[0021] The residual gas D after the mixed gas C is purified in step S130 is also subjected to tail gas treatment by the tail gas treatment system; preferably, the residual gas D is mixed with air and methanol fuel in the premixer II and sent to the combustion chamber for combustion; the hot flue gas generated by the combustion is respectively heat-exchanged with the gasifier and the reformer, and then treated in the tail gas processor.

[0022] According to a preferred embodiment of the present invention, the purifier adopts PSA pressure swing adsorption or membrane separation technology for purification, with a purification rate higher than 85% and a purity of 99.999%.

[0023] The present application uses steam provided by a light water nuclear reactor as a hydrogen production raw material and combines it with a pressure swing adsorption method to purify hydrogen, thereby obtaining hydrogen with a purity of up to 99.999%, and achieving a stable and efficient hydrogen supply.

[0024] According to a preferred embodiment of the present invention, in step S130, cooling circulating water is used to cool the mixed gas B, and the inlet temperature of the cooling circulating water is 15-32°C, and the outlet temperature is 33-45°C.

[0025] According to a preferred embodiment of the present invention, the temperature of the hot flue gas is 390-420°C;

[0026] Preferably, the ratio of the heat supply of the hot flue gas to the gasifier to the heat supply to the reformer is (0.7-0.9):1.

[0027] According to a preferred embodiment of the present invention, the light water reactor unit comprises a light water reactor, a steam generator, a steam turbine and a power supply device, wherein the light water reactor provides heat energy for the steam generator to produce water vapor; the water vapor produced by a part of the steam generator is used to provide water vapor raw material for the reforming hydrogen production unit, and the remaining part of the water vapor drives the steam turbine to rotate and generate electric energy, which is transported to the reforming hydrogen production unit by the power supply device;

[0028] Preferably, the temperature of the water vapor at the steam generator outlet is 220-300°C.

[0029] The heat energy generated by the light water reactor of the present application acts on the steam generator, and the steam generator generates water vapor. Part of the water vapor is used as a water vapor raw material, and the remaining part is converted into electrical energy by a steam turbine. The water vapor raw material used to provide the reforming hydrogen production unit accounts for 1-3% of the total water vapor flow, preferably 1.2-1.6, and more preferably 1.5%. The water vapor that drives the steam turbine to rotate and generate electricity accounts for 45-60% of the total water vapor, preferably 52-60%, and more preferably 53-56%. A stable supply of water vapor and electricity to the light water reactor can be achieved, ensuring the effective and normal operation of the nuclear energy hydrogen production system.

[0030] In a certain embodiment of the present application, the reforming hydrogen production unit further includes a nitrogen storage tank for purging the entire system.

[0031] The beneficial effects of the present invention are as follows: the present invention combines a light water nuclear reactor with methanol steam reforming to produce hydrogen, which can effectively improve the comprehensive utilization capacity of nuclear energy and improve the economic efficiency of the nuclear reactor.

[0032] The steam outlet temperature of the light water reactor is regulated to 220-300℃. The light water reactor can be used in conjunction with the methanol steam reforming unit to achieve simple and efficient energy and fuel supply. The methanol conversion rate and hydrogen production rate of reforming hydrogen are high, which can effectively improve the heat exchange efficiency of the reforming hydrogen production process. BRIEF DESCRIPTION OF THE DRAWINGS

[0033] Figure 1 This is the relationship between hydrogen mass ratio and pressure (MPa) at different temperatures for methanol steam reforming;

[0034] Figure 2 This is the relationship between the mass ratio of byproduct carbon monoxide and pressure (MPa) at different temperatures in methanol steam reforming;

[0035] Figure 3 This is the relationship between hydrogen production rate and water-to-methanol ratio at different temperatures and working pressure of 1.1MPa;

[0036] Figure 4 A schematic diagram of the methanol steam reforming hydrogen production process of this application;

[0037] Figure 5 This is a schematic diagram of the methanol steam reforming hydrogen production process in Example 1. DETAILED DESCRIPTION

[0038] The present invention will be further described below in conjunction with specific embodiments, but they do not constitute any limitation to the present invention.

[0039] like Figure 4As shown, the methanol steam reforming hydrogen production process of the present application combines a light water reactor unit with a reforming hydrogen production unit; the light water reactor unit is used to provide steam raw materials and electrical energy for the reforming hydrogen production unit.

[0040] The light water reactor unit provides water vapor raw material, and optional electric energy. Raw material methanol (temperature 25-35℃, pressure 0.5-1.5bar) and water vapor raw material (temperature 240-260℃, pressure 20-25bar) are transported to premixer I through pipelines. Raw material methanol is in liquid state. Raw material methanol is mixed with water vapor raw material with higher temperature (the mass flow ratio of water vapor to methanol is 0.6-0.7) to obtain mixed raw material A; the gasifier further increases the temperature of mixed raw material A, and the gasification temperature is higher than the boiling point of methanol, so that methanol is completely gasified; and then enters the reformer. Methanol and water vapor are reformed in the reformer at a reforming temperature of 240-280℃, a reforming pressure of 5-15bar, and a water-to-methanol mass ratio of (0.6-0.7):1 to generate a mixed gas B of hydrogen and carbon dioxide as a product. The mixed gas B enters the gas-liquid separator, and the gas-liquid separator uses cooling circulating water to cool the reformed gas. The inlet temperature of the cooling circulating water is 15-32°C, and the outlet temperature is 33-45°C. The temperature of the cooling circulating water is lower than the boiling points of methanol and water. After the mixed gas B is treated by the gas-liquid separator, the unreacted methanol and water can be effectively removed. The remaining mixed gas C is purified by a purifier to obtain hydrogen (purification rate higher than 85%, purity 99.999%) and remaining gas D.

[0041] The remaining gas D is mixed with air and methanol fuel in the premixer II and enters the combustion chamber for combustion. The hot flue gas obtained is used to heat the mixed raw materials in the gasifier and reformer, and is finally discharged after tail gas treatment. The flow ratio of methanol raw material to methanol fuel is (2.55-3.4):1. The temperature of the hot flue gas is 390-420℃; the hot flue gas exchanges heat with the gasifier and reformer respectively, and the ratio of the heat supply to the gasifier to the heat supply to the reformer is (0.7-0.9):1.

[0042] [Example 1]

[0043] like Figure 5 As shown, the light water reactor produces 245℃, 21bar steam, of which 6.4*10 3 Kg / h as steam raw material. 1.02*10 4 Kg / h, 1bar raw methanol and steam raw material are mixed in premixer I to obtain 1.66*10 4Kg / h, 156℃, 11bar mixed raw material A, mixed raw material A is heated to 245℃ by the gasifier and sent to the reformer. The methanol raw material reacts with water vapor in the reformer to obtain a mixed gas B of hydrogen and carbon dioxide, wherein the temperature in the reformer is 245℃, the pressure is 11bar, and the water-to-alcohol mass ratio is 0.627. Mixed gas B enters the gas-liquid separator to remove unreacted liquefied methanol and water, and the remaining mixed gas C is purified by the purifier to obtain a hydrogen output of 20000Nm 3 / h, the hydrogen yield is 94.80%, the purification rate is 90%, and the purity is 99.999%.

[0044] The heat exchange efficiency of the reformer in this embodiment is 97.42%, and the methanol conversion rate is 98.34%.

[0045] The hydrogen yield is defined as (z, %)

[0046]

[0047] Where n is the molar flow rate;

[0048] The heat transfer efficiency of the reformer is defined as (w, %)

[0049]

[0050] Where Q is the calorific value, Q 重整 Heat absorbed for reforming;

[0051] Methanol conversion is defined as (x, %)

[0052]

[0053] Where n is the molar flow rate.

[0054] [Example 2]

[0055] The difference from Example 1 is that the reforming temperature is 255°C and the hydrogen production is 20439Nm 3 / h, the hydrogen yield is 94.81%, the purification rate is 90%, and the purity is 99.999%.

[0056] The heat exchange efficiency of the reformer in this embodiment is 97.32%, and the methanol conversion rate is 98.58%.

[0057] [Example 3]

[0058] The difference from Example 1 is that the reforming temperature is 250°C and the hydrogen production is 20438Nm 3 / h, the hydrogen yield is 94.81%, the purification rate is 90%, and the purity is 99.999%.

[0059] The heat exchange efficiency of the reformer in this embodiment is 97.32%, and the methanol conversion rate is 98.60%.

[0060] [Example 4]

[0061] The difference from Example 1 is that the reforming temperature is 248°C and the hydrogen production is 20439Nm 3 / h, the hydrogen yield is 94.81%, the purification rate is 90%, and the purity is 99.999%.

[0062] The heat exchange efficiency of the reformer in this embodiment is 97.35%, and the methanol conversion rate is 98.49%.

[0063] [Example 5]

[0064] The difference from Example 1 is that the reforming temperature is 242°C and the hydrogen production is 20431Nm 3 / h, the hydrogen yield is 94.77%, the purification rate is 90%, and the purity is 99.999%.

[0065] The heat exchange efficiency of the reformer in this embodiment is 97.40%, and the methanol conversion rate is 98.17%.

[0066] [Example 6]

[0067] The difference from Example 1 is that the reforming temperature is 240°C and the hydrogen production is 20426Nm 3 / h, the hydrogen yield is 94.75%, the purification rate is 90%, and the purity is 99.999%.

[0068] The heat exchange efficiency of the reformer in this embodiment is 97.41%, and the methanol conversion rate is 98.06%.

[0069] [Example 7]

[0070] The difference from Example 1 is that the reforming temperature is 235°C and the hydrogen production is 20405Nm 3 / h, the hydrogen yield is 94.65%, the purification rate is 90%, and the purity is 99.999%.

[0071] The heat exchange efficiency of the reformer in this embodiment is 97.40%, and the methanol conversion rate is 97.73%.

[0072] The parameters of Examples 1-7 are shown in Table 1 below:

[0073] Table 1

[0074] <![CDATA[Hydrogen production volume Nm 3 / h]]> Hydrogen yield% Heat transfer efficiency % Methanol conversion rate % Example 1 20436 94.80％ 97.42％ 98.34％ Example 2 20439 94.81％ 97.32％ 98.58％ Example 3 20438 94.81％ 97.32％ 98.60％ Example 4 20439 94.81％ 97.35％ 98.49％ Example 5 20431 94.77％ 97.40％ 98.34％ Example 6 20426 94.75％ 97.41％ 98.06％ Example 7 20405 94.65％ 97.40％ 97.73％

[0075] Cost comparison:

[0076] Comparison of the economic efficiency of hydrogen production by light water reactor combined with methanol reforming and hydrogen production by light water reactor combined with water electrolysis: the equipment has been in operation for 10 years, with 8,000 operating hours per year.

[0077] The cost of hydrogen production by combining SMR light water reactor with methanol reforming in this application is 2.01-2.64 yuan / Nm 3 H 2 .

[0078] The cost of using SMR light water reactor combined with water electrolysis to produce hydrogen is 3.35-3.80 yuan / Nm 3 H 2 .

[0079] After analyzing the calculation results, it was found that when the price of methanol fluctuates greatly (the cost of methanol is mainly related to the mode of transportation, the higher the transportation cost, the higher the cost of methanol), the cost of hydrogen production by SMR light water reactor combined with methanol reforming is still lower than the cost of SMR light water reactor combined with water electrolysis.

[0080] Therefore, the SMR light water reactor combined with methanol reforming hydrogen production system of the present application is significantly superior to the SMR combined with water electrolysis hydrogen production system in terms of economy, thermal efficiency and hydrogen production efficiency.

[0081] The advantage of the process of this application is that the optimal operating temperature of the SMR light water reactor coupled with methanol reforming hydrogen production system is determined to be 240℃-250℃, and the optimal operating pressure is 1.1MPa. This application proposes a technology for using a light water reactor for methanol reforming reaction, thereby expanding the way of low-temperature nuclear energy hydrogen production, supporting the comprehensive utilization of nuclear energy, supplementing the supply of hydrogen, and helping to meet the challenges brought by global climate change.

[0082] Any numerical value mentioned in the present invention, if there is only an interval of two units between any minimum value and any maximum value, includes all values ​​from the minimum value to the maximum value each time increasing by one unit. For example, if the amount of a component, or the value of a process variable such as temperature, pressure, time, etc. is declared to be 50-90, in this specification it means that 51-89, 52-88... and 69-71 and 70-71 are specifically listed. For non-integer values, 0.1, 0.01, 0.001 or 0.0001 can be appropriately considered as a unit. These are just some specially specified examples. In this application, in a similar manner, all possible combinations of numerical values ​​between the listed minimum and maximum values ​​are considered to have been disclosed.

[0083] It should be noted that the embodiments described above are only used to explain the present invention and do not constitute any limitation to the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words, rather than restrictive words. The present invention may be modified as specified within the scope of the claims of the present invention, and the present invention may be revised without departing from the scope and spirit of the present invention. Although the present invention described therein relates to specific methods, materials and embodiments, it does not mean that the present invention is limited to the specific examples disclosed therein, on the contrary, the present invention can be extended to all other methods and applications with the same functions.

Claims

1. A process for producing hydrogen by methanol steam reforming coupled to a nuclear reactor, characterized in that: A light water reactor unit is used in conjunction with a reforming hydrogen production unit; the light water reactor unit provides water vapor raw material and optional electrical energy for the reforming hydrogen production unit.

2. The methanol steam reforming hydrogen production process according to claim 1, characterized in that: The reforming hydrogen production unit comprises a premixer I, a gasifier, a reformer, a gas-liquid separator and a purifier; the process comprises the following steps: S110, mixing a steam raw material from a light water reactor unit with a methanol raw material in a premixer I to obtain a mixed raw material A; S120, sending the mixed raw material A into a gasifier for gasification, and then into a reformer for reforming to obtain a mixed gas B containing hydrogen and carbon dioxide; S130, sending the mixed gas B to a gas-liquid separator for treatment to obtain a mixed gas C, and the mixed gas C is purified by a purifier to obtain hydrogen.

3. The methanol steam reforming hydrogen production process according to claim 2, characterized in that: The reforming conditions in step S120 include: a reforming temperature of 200-350°C, preferably 240-280°C, more preferably 240-255°C; a reforming pressure of 5-15 bar, preferably 10-12 bar; and a water-to-alcohol mass ratio of (0.6-0.8):1, preferably (0.6-0.7):

1.

4. The process for producing hydrogen by methanol steam reforming according to claim 2, characterized in that: In step S120, the temperature of the mixed raw material A when it is fed into the gasifier is 150-180°C, preferably 150-160°C.

5. The process for producing hydrogen through methanol steam reforming according to any one of claims 2 to 4, characterized in that: In step S110, the temperature of the methanol raw material entering the premixer I is 25-35°C, and the pressure is 0.5-1.5 bar; the temperature of the water vapor raw material is 240-260°C, and the pressure is 20-25 bar; the mass flow ratio of the water vapor raw material to the methanol raw material is (0.6-0.7):

1.

6. The process for producing hydrogen through methanol steam reforming according to any one of claims 2 to 4, characterized in that: The reforming hydrogen production unit further includes a residual tail gas treatment system; preferably, the residual tail gas treatment system includes a premixer II, a combustion chamber and a tail gas processor; The residual gas D after the mixed gas C is purified in step S130 is also subjected to tail gas treatment by the tail gas treatment system; preferably, the residual gas D is mixed with air and methanol fuel in the premixer II and sent to the combustion chamber for combustion; the hot flue gas generated by the combustion is respectively heat-exchanged with the gasifier and the reformer, and then treated in the tail gas processor.

7. The process for producing hydrogen through methanol steam reforming according to any one of claims 2 to 4, characterized in that: The purifier adopts PSA pressure swing adsorption or membrane separation technology for purification, and the purification rate is higher than 85%.

8. The process for producing hydrogen through methanol steam reforming according to any one of claims 2 to 4, characterized in that: In step S130, the mixed gas B is cooled by cooling circulating water, wherein the inlet temperature of the cooling circulating water is 15-32°C and the outlet temperature is 33-45°C.

9. The process for producing hydrogen by methanol steam reforming according to claim 6, characterized in that: The temperature of the hot flue gas is 390-420°C; Preferably, the ratio of the heat supply of the hot flue gas to the gasifier to the heat supply to the reformer is (0.7-0.9):

1.

10. The process for producing hydrogen through methanol steam reforming according to any one of claims 1 to 4, characterized in that: The light water reactor unit includes a light water reactor, a steam generator, a steam turbine and a power supply device. The light water reactor provides heat energy for the steam generator to produce water vapor; part of the water vapor produced by the steam generator is used to provide water vapor raw materials for the reforming hydrogen production unit, and the remaining part of the water vapor drives the steam turbine to rotate to generate electricity, which is transported to the reforming hydrogen production unit by the power supply device; Preferably, the temperature of the water vapor at the steam generator outlet is 220-300°C.

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