Low-consumption methanol hydrogen production system

Abstract

The utility model relates to the field of chemical engineering, in particular to a low-consumption methanol hydrogen production system. According to the cracking reaction tank provided by the utility model, the two reaction areas are arranged, and methanol steam respectively reacts in the reaction tubes of the two reaction areas, so that the reaction path of the methanol steam in the catalytic cracking reaction is prolonged, and the reaction efficiency is improved. Meanwhile, the conduction oil is heated by the conduction oil boiler, and the heated conduction oil enters the reaction area and can uniformly provide heat for the cracking reaction of the methanol steam, so that the problem of low reaction efficiency caused by non-uniform heating is avoided. The methanol steam generates high-temperature mixed hydrogen in the cracking reaction tank, and the high-temperature mixed hydrogen and the liquid methanol are thermally coupled in the heat exchanger, so that the temperature of the liquid methanol can be increased, the heat required during vaporization is further reduced, and meanwhile, the temperature of the thermally coupled mixed hydrogen is reduced, so that the use amount of cooling water can be reduced.

Description

Technical Field

[0001] The utility model relates to the field of chemical industry, in particular to a low-consumption methanol hydrogen production system. Background Art

[0002] The information disclosed in this background technology section is only intended to increase understanding of the overall background of the present invention, and is not necessarily regarded as an admission or any form of suggestion that the information constitutes the prior art already known to those skilled in the art.

[0003] Hydrogen has a wide range of uses in industry. In recent years, due to the rapid development of fine chemicals, anthraquinone method for producing hydrogen peroxide, powder metallurgy, oil hydrogenation, forestry and agricultural product hydrogenation, bioengineering, petroleum refining hydrogenation, and hydrogen-fueled clean vehicles, the demand for pure hydrogen has increased rapidly.

[0004] At present, the main methods of hydrogen production include hydrogen production by the reaction of steam and hydrogen production catalysts, hydrogen production by fossil fuel reforming, hydrogen production by water electrolysis, hydrogen production by photohydrolysis, biological hydrogen production, and plasma hydrogen production. Among them, the most widely used method of hydrogen production is to use methanol to produce hydrogen. Methanol hydrogen production refers to the use of methanol solution as a raw material under certain temperature and pressure conditions. Methanol is heated to produce methanol vapor, and then the methanol vapor undergoes a conversion reaction under the action of a hydrogen production catalyst to finally produce hydrogen. However, the existing methanol hydrogen production technology has problems such as uneven heating of methanol during vaporization, short methanol vapor path in the catalytic cracking reaction, and uneven heating of the catalyst, resulting in incomplete cracking reaction and low overall reaction efficiency. Furthermore, there is no energy recovery and utilization in the hydrogen production process, resulting in high energy consumption. Utility Model Content

[0005] In order to solve the above problems, the utility model provides a low-consumption methanol hydrogen production system.

[0006] In order to achieve the above technical objectives, the present invention adopts the following technical solutions:

[0007] A low-consumption methanol hydrogen production system comprises a methanol liquid storage tank, which is sequentially connected to a heat exchanger, a methanol vaporizer, and a cracking reaction tank;

[0008] The cracking reaction tank includes a reaction tank body, which is provided with a buffer chamber, an air inlet chamber, an air outlet chamber and a reaction zone, wherein the buffer chamber is located at the top of the reaction zone, and the air inlet chamber and the air outlet chamber are arranged side by side at the bottom of the reaction zone; the reaction zone includes a first reaction zone and a second reaction zone; a plurality of first reaction tubes are evenly distributed in the first reaction zone, wherein the top ends of the plurality of first reaction tubes are connected to the buffer zone, and the bottom ends of the plurality of first reaction tubes are connected to the air inlet chamber; a plurality of second reaction tubes are evenly distributed in the second reaction zone, wherein the top ends of the plurality of second reaction tubes are connected to the buffer zone, and the bottom ends of the plurality of second reaction tubes are connected to the air outlet chamber;

[0009] The air outlet cavity is provided with an air outlet, and the air outlet is connected to the heat exchanger.

[0010] In one or some embodiments of the present invention, the methanol vaporizer includes a vaporizer body, wherein the vaporizer body is a jacketed structure;

[0011] A liquid methanol inlet is provided at the lower portion of the outer casing, and a methanol vapor outlet is provided at the upper portion of the outer casing;

[0012] Preferably, a heating tube is provided at the bottom of the inner casing.

[0013] In one or some embodiments of the present invention, the reaction tank body is provided with a first baffle and a second baffle, wherein the first baffle is located between the buffer zone and the reaction zone; the second baffle is located between the reaction zone and the air inlet cavity and the air outlet cavity;

[0014] Preferably, the top end of the first reaction tube passes through the first baffle and is connected to the buffer chamber; the bottom end of the first reaction tube passes through the second baffle and is connected to the air inlet chamber;

[0015] Preferably, the top end of the second reaction tube passes through the first baffle and is connected to the buffer chamber; the bottom end of the second reaction tube passes through the second baffle and is connected to the gas outlet chamber.

[0016] In one or some embodiments of the present invention, the cracking reaction tank is connected to a thermal oil boiler.

[0017] Preferably, a heat transfer oil inlet is provided at the lower portion of the reaction zone of the cracking reaction tank, and a heat transfer oil outlet is provided at the upper portion of the reaction zone of the cracking reaction tank;

[0018] Further preferably, the thermal oil boiler is provided with a thermal oil boiler outlet and a thermal oil boiler inlet; the thermal oil inlet is connected to the thermal oil boiler outlet; and the thermal oil outlet is connected to the thermal oil boiler inlet.

[0019] In one or some embodiments of the present invention, the heat exchanger is connected to a water condenser; and the water condenser is connected to an automatic drainer.

[0020] Preferably, the automatic drainer is connected to the gas separation device and the hydrogen storage tank in sequence.

[0021] The beneficial effects of the present invention are:

[0022] (1) The cracking reaction tank provided by the present invention is provided with two reaction zones, and methanol vapor reacts in the reaction tubes of the two reaction zones, respectively, thereby extending the reaction path of the methanol vapor in the catalytic cracking reaction and improving the reaction efficiency. At the same time, the thermal oil boiler heats the thermal oil, and the heated thermal oil enters the reaction zone to uniformly provide heat to the cracking reaction of the methanol vapor, thereby avoiding the problem of low reaction efficiency caused by uneven heating.

[0023] (2) The high-temperature mixed hydrogen generated by methanol vapor in the cracking reactor is thermally coupled with liquid methanol in the heat exchanger, which not only increases the temperature of the liquid methanol and reduces the heat required for vaporization, but also reduces the temperature of the mixed hydrogen after thermal coupling, which can reduce the amount of cooling water used. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The drawings in the specification, which constitute a part of the present invention, are used to provide a further understanding of the present invention. The illustrative embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation on the present invention.

[0025] Figure 1 This is the system structure diagram of the utility model;

[0026] Figure 2 is a cross-sectional view of the cracking reaction tank (cut along the second baffle);

[0027] Among them, 1 is a methanol storage tank, 2 is a metering pump, 3 is a heat exchanger, 4 is a methanol vaporizer, 5 is a cracking reaction tank, 5-1 is a buffer chamber, 5-2 is a reaction zone, 5-3 is an air inlet chamber, 5-4 is an air outlet chamber, 5-5 is a first baffle, 5-6 is a second baffle, 5-2-1 is a first reaction tube, 5-2-2 is a second reaction tube, 6 is a thermal oil boiler, 7-water condenser, 8-automatic drainer, 9-gas separation device, 10-hydrogen storage tank. DETAILED DESCRIPTION

[0028] It should be noted that the following detailed descriptions are exemplary and are intended to provide further explanation of the present invention. Unless otherwise specified, all technical and scientific terms used in the present invention have the same meanings as those commonly understood by those skilled in the art to which the present invention belongs.

[0029] It should be noted that the terms used herein are only for describing specific embodiments and are not intended to limit the exemplary embodiments according to the present invention. As used herein, unless the context clearly indicates otherwise, the singular form is also intended to include the plural form. In addition, it should be understood that when the terms "comprise" and / or "include" are used in this specification, they indicate the presence of features, steps, operations, devices, components and / or combinations thereof.

[0030] The present invention will be further described in detail below in conjunction with specific embodiments. It should be noted that the specific embodiments are intended to explain rather than limit the present invention.

[0031] Example 1

[0032] See also Figure 1 A low-consumption methanol hydrogen production system includes a methanol storage tank 1, which is sequentially connected to a heat exchanger 3, a methanol vaporizer 4, and a cracking reaction tank 5;

[0033] The cracking reaction tank 5 includes a reaction tank body, which is provided with a buffer chamber 5-1, an air inlet chamber 5-3, an air outlet chamber 5-4 and a reaction zone 5-2. The buffer chamber 5-1 is located at the top of the reaction zone 5-2, and the air inlet chamber 5-3 and the air outlet chamber 5-4 are arranged side by side at the bottom of the reaction zone 5-2; the reaction zone 5-2 includes a first reaction zone and a second reaction zone; a plurality of first reaction tubes 5-2-1 are evenly distributed in the first reaction zone, the top ends of the plurality of first reaction tubes 5-2-1 are connected to the buffer zone 5-1, and the bottom ends of the plurality of first reaction tubes 5-2-1 are connected to the air inlet chamber 5-4; a plurality of second reaction tubes 5-2-2 are evenly distributed in the second reaction zone, the top ends of the plurality of second reaction tubes 5-2-2 are connected to the buffer zone 5-1, and the bottom ends of the plurality of second reaction tubes 5-2-2 are connected to the air outlet chamber 5-4;

[0034] The air outlet cavity 5 - 4 is provided with an air outlet, which is connected to the heat exchanger 3 .

[0035] The methanol vaporizer 4 includes a vaporizer body having a jacketed structure; a liquid methanol inlet is provided at the bottom of the outer jacket, and a methanol vapor outlet is provided at the top of the outer jacket; and a heating pipe is provided at the bottom of the inner jacket. The inner jacket is filled with heat transfer oil, and liquid methanol enters the interlayer space between the inner and outer jackets through the liquid methanol inlet at the bottom of the outer jacket. The heating pipe provided at the bottom of the inner jacket heats the heat transfer oil, which transfers heat to the methanol, thereby vaporizing the methanol to generate methanol vapor, which flows out through the methanol vapor outlet at the top of the outer jacket. Liquid methanol has a higher density than methanol vapor and therefore settles under the action of gravity. Therefore, the methanol vapor overflowing from the methanol vapor outlet at the top of the outer jacket contains almost no liquid methanol, which facilitates improving the efficiency of the subsequent cracking reaction.

[0036] The reactor body is equipped with a first baffle 5-5 and a second baffle 5-6. The first baffle 5-5 is located between the buffer zone 5-1 and the reaction zone 5-2; the second baffle 5-6 is located between the reaction zone 5-2 and the air inlet chamber 5-3 and the air outlet chamber 5-4. The air inlet chamber 5-3 and the air outlet chamber 5-4 are not connected to each other. The top end of the first reaction tube 5-2-1 passes through the first baffle 5-5 and is connected to the buffer zone 5-1; the bottom end of the first reaction tube 5-2-1 passes through the second baffle 5-6 and is connected to the air inlet chamber 5-3; the top end of the second reaction tube 5-2-2 passes through the first baffle 5-5 and is connected to the buffer zone 5-1; the bottom end of the second reaction tube 5-2-2 passes through the second baffle 5-6 and is connected to the air outlet chamber 5-3. Methanol vapor enters the first reaction tube 5-2-1 through the air inlet chamber 5-3, undergoes cracking under the catalytic influence of the catalyst supported on the inner wall of the first reaction tube 5-2-1, then enters the buffer zone 5-1 and the second reaction tube 5-2-2, where it undergoes further reaction under the catalytic influence of the catalyst supported on the inner wall of the second reaction tube 5-2-1. The cracking reactor 5 is provided with two reaction zones, with the methanol vapor reacting in the reaction tubes of each zone, respectively. This extends the reaction path of the methanol vapor during the catalytic cracking reaction and improves reaction efficiency.

[0037] The cracking reactor 5 is connected to a thermal oil boiler 6. A thermal oil inlet is provided at the bottom of the reaction zone 5-2 of the cracking reactor 5, and a thermal oil outlet is provided at the top of the reaction zone 5-2 of the cracking reactor 5. The thermal oil boiler 6 is provided with a thermal oil boiler outlet and a thermal oil boiler inlet. The thermal oil inlet is connected to the thermal oil boiler outlet, and the thermal oil outlet is connected to the thermal oil boiler inlet. The thermal oil boiler 6 heats the thermal oil. The heated thermal oil enters the reaction zone 5-2 of the cracking reactor 5 through the thermal oil inlet, providing heat for the cracking reaction of the methanol vapor. The thermal oil then returns from the thermal oil outlet to the thermal oil boiler 6 for further heating, allowing for recycling. The use of thermal oil can evenly provide heat to the cracking reaction of the methanol vapor, avoiding the problem of low reaction efficiency caused by uneven heating.

[0038] Heat exchanger 3 includes a methanol inlet and a methanol outlet; a methanol storage tank 1 is connected to the methanol inlet via a metering pump 2; the methanol outlet is connected to a methanol vaporizer 4; a mixed hydrogen inlet and a mixed hydrogen outlet are connected to the outlet of gas outlet chamber 5-4; and the mixed hydrogen outlet is connected to a water condenser 7. Methanol vapor in the cracking reactor 5 generates high-temperature mixed hydrogen. Thermal coupling of the high-temperature mixed hydrogen with liquid methanol occurs within heat exchanger 3, raising the temperature of the liquid methanol and reducing the heat required for vaporization. This thermal coupling also lowers the temperature of the mixed hydrogen, reducing cooling water usage.

[0039] The heat exchanger 3 is connected to the water condenser 7; the water condenser 7 is connected to the automatic drain 8; the automatic drain 8 is connected in turn to the gas separation device 9 and the hydrogen storage tank 10. Specifically, the automatic drain 8 includes a gas outlet and a liquid outlet, the liquid outlet is connected to the methanol storage tank 1; the gas outlet is connected to the gas separation device 9. After thermal coupling, the mixed hydrogen enters the water condenser 7 for cooling, and after cooling, a gas-liquid mixture is produced, where the liquid is unreacted methanol and the gas is a mixture of gases such as hydrogen and carbon monoxide; the gas-liquid mixture enters the automatic drain 8, the unreacted methanol liquid enters the methanol storage tank 1, and the gas enters the gas separation device 9 for separation to obtain hydrogen, which eventually enters the hydrogen storage tank 10 for storage.

[0040] The process is:

[0041] The liquid methanol in the methanol storage tank 1 enters the heat exchanger 3 through a metering pump, where the high-temperature mixed hydrogen generated by the cracking of the methanol vapor in the cracking reaction tank 5 will be thermally coupled with the liquid methanol in the heat exchanger 3 to increase the temperature of the liquid methanol; the liquid methanol enters the interlayer space between the inner and outer layers of the methanol vaporizer 4, and the heating pipe arranged at the bottom of the inner shell will heat the heat transfer oil. The heated heat transfer oil transfers heat to the methanol, thereby vaporizing the methanol to generate methanol vapor, which flows out through the methanol vapor outlet at the top of the outer shell; the methanol vapor enters the first reaction tube 5-2-1 through the air inlet cavity 5-3, and is cracked under the catalysis of the catalyst loaded on the inner wall of the first reaction tube 5-2-1, and then enters the buffer zone 5-1, and then enters The methanol vapor in the cracking reaction tank 5 generates high-temperature mixed hydrogen. The high-temperature mixed hydrogen and liquid methanol are thermally coupled in the heat exchanger 3. The coupled mixed hydrogen enters the water condenser 7 for cooling. After cooling, a gas-liquid mixture is generated, in which the liquid is unreacted methanol and the gas is a mixed gas containing hydrogen, carbon monoxide and other gases. The gas-liquid mixture enters the automatic drainer 8, the unreacted methanol liquid enters the methanol storage tank 1, and the gas enters the gas separation device 9 for separation to obtain hydrogen, and the hydrogen finally enters the hydrogen storage tank 10 for storage.

[0042] Finally, it should be noted that the above description is merely a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art will be able to modify the technical solutions described in the aforementioned embodiments or replace parts of them with equivalents. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principles of the present invention shall be included within the scope of protection of the present invention.

Claims

1. A low-consumption methanol hydrogen production system, characterized in that: It includes a methanol storage tank, which is sequentially connected to a heat exchanger, a methanol vaporizer, and a cracking reaction tank; The cracking reaction tank includes a reaction tank body, which is provided with a buffer chamber, an air inlet chamber, an air outlet chamber and a reaction zone, wherein the buffer chamber is located at the top of the reaction zone, and the air inlet chamber and the air outlet chamber are arranged side by side at the bottom of the reaction zone; the reaction zone includes a first reaction zone and a second reaction zone; a plurality of first reaction tubes are evenly distributed in the first reaction zone, wherein the top ends of the plurality of first reaction tubes are connected to the buffer zone, and the bottom ends of the plurality of first reaction tubes are connected to the air inlet chamber; a plurality of second reaction tubes are evenly distributed in the second reaction zone, wherein the top ends of the plurality of second reaction tubes are connected to the buffer zone, and the bottom ends of the plurality of second reaction tubes are connected to the air outlet chamber; The air outlet cavity is provided with an air outlet, and the air outlet is connected to the heat exchanger.

2. The low-consumption methanol hydrogen production system according to claim 1, characterized in that: The methanol vaporizer comprises a vaporizer body, which is a jacketed structure.

3. The low-consumption methanol hydrogen production system according to claim 2, characterized in that: A liquid methanol inlet is provided at the lower portion of the outer casing, and a methanol vapor outlet is provided at the upper portion of the outer casing; A heating pipe is arranged at the bottom of the inner sleeve.

4. The low-consumption methanol hydrogen production system according to claim 1, characterized in that: The reaction tank body is provided with a first baffle and a second baffle, wherein the first baffle is located between the buffer zone and the reaction zone; the second baffle is located between the reaction zone and the air inlet cavity and the air outlet cavity.

5. The low-consumption methanol hydrogen production system according to claim 4, characterized in that: The top end of the first reaction tube passes through the first baffle and is connected to the buffer chamber; the bottom end of the first reaction tube passes through the second baffle and is connected to the air inlet chamber.

6. The low-consumption methanol hydrogen production system according to claim 4, characterized in that: The top end of the second reaction tube passes through the first baffle and is connected to the buffer chamber; the bottom end of the second reaction tube passes through the second baffle and is connected to the gas outlet chamber.

7. The low-consumption methanol hydrogen production system according to claim 1, characterized in that: The cracking reaction tank is connected to the thermal oil boiler.

8. The low-consumption methanol hydrogen production system according to claim 7, characterized in that: The lower part of the reaction zone of the cracking reaction tank is provided with a heat transfer oil inlet, and the upper part of the reaction zone of the cracking reaction tank is provided with a heat transfer oil outlet; The thermal oil boiler is provided with a thermal oil boiler outlet and a thermal oil boiler inlet; the thermal oil inlet is connected to the thermal oil boiler outlet; the thermal oil outlet is connected to the thermal oil boiler inlet.

9. The low-consumption methanol hydrogen production system according to claim 1, characterized in that: The heat exchanger is connected to the water condenser; and the water condenser is connected to the automatic drainer.

10. The low-consumption methanol hydrogen production system according to claim 9, characterized in that: The automatic drainer is connected to the gas separation device and the hydrogen storage tank in sequence.

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