Methanol-to-hydrogen synergistic hydrogen combustion evaporator
By adopting hydrogen reverse combustion technology in the methanol hydrogen production synergistic hydrogen combustion evaporator, the pollution and high energy consumption problems of traditional methanol combustion boilers are solved, and pollution-free and high-efficiency methanol hydrogen production and steam production are achieved.
Patent Information
- Application Number
- CN202422624207.8
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-10-30
- Publication Date
- 2025-06-13
- Estimated Expiration
- 2034-10-30
AI Technical Summary
Traditional methanol combustion boilers have problems with pollutant emissions and high energy consumption, and methanol hydrogen production equipment requires additional heating devices to maintain stable and efficient hydrogen production.
A synergistic hydrogen combustion evaporator for methanol hydrogen production is designed, and the reverse combustion technology of hydrogen as fuel is adopted. The high-temperature gas is driven from top to bottom through the fan to increase the contact time with the evaporator, methanol evaporator, etc., and improve the heat transfer efficiency.
Pollutant-free emissions are achieved, energy consumption and fuel costs are significantly reduced, and the high temperature of methanol steam is enough to maintain the stable operation of methanol hydrogen production catalytic reaction, reducing the cost of equipment maintenance and environmental protection treatment.
Smart Images
Figure CN222978106U_ABST
Abstract
Description
Technical Field
[0001] The present invention relates to the field of high-temperature steam equipment, and more particularly to a methanol-to-hydrogen synergy hydrogen combustion evaporator. Background Art
[0002] Methanol is widely sourced and has a mature production process. It is mainly derived from coal chemical industry and natural gas synthesis, and can be produced from coal, natural gas, coalbed methane, biomass, etc. Comparing the physical and chemical properties of methanol with other fuels, it has the following characteristics: 1. Low calorific value, the calorific value of methanol is about half of that of gasoline. 2. Toxic, methanol is highly toxic and not suitable for drinking. 3. Under high temperature and sufficient air conditions, complete combustion of methanol produces CO 2 and H 2 O. However, during methanol combustion, pollutants such as formaldehyde and nitrogen oxides can also be generated, and further purification treatment is required. 4. The cost of generating unit heat from methanol is relatively low, so methanol can be used as a gasoline additive to reduce fuel costs. A new type of green and environmentally friendly fuel boiler using methanol as fuel has thus emerged, and its nitrogen oxide emissions can be less than 30 mg. However, this boiler still emits pollutants. Summary of the Invention
[0003] The object of the present invention is to overcome the deficiencies of the above-mentioned traditional technologies, and to provide a methanol-to-hydrogen synergy hydrogen combustion evaporator that uses hydrogen as fuel, has no pollutant emissions, is highly efficient, has a low usage cost, and can cooperate with methanol-to-hydrogen equipment.
[0004] The object of the present invention is achieved by the following technical measures:
[0005] Methanol-to-hydrogen co-combustion evaporator, comprising an air chamber and a combustion chamber, characterized in that the lower part of the air chamber is communicated with the upper part of the combustion chamber, the lower part of the combustion chamber is provided with an air outlet, and a hydrogen burner, an evaporator, a methanol evaporator, a medium-temperature heater and a condenser are sequentially arranged in the combustion chamber from top to bottom. The hydrogen burner is arranged between the air chamber and the combustion chamber, and the combustion direction of the hydrogen burner faces the evaporator below. The water inlet end of the condenser is connected with a water pump, the water outlet end of the condenser is communicated with the water inlet end of the medium-temperature heater, the water outlet end of the medium-temperature heater is communicated with the water inlet end of the evaporator, the liquid inlet end of the methanol evaporator is communicated with a methanol storage tank through a methanol pump, the liquid outlet end of the methanol evaporator is connected with a methanol vapor pipe, and the gas inlet end of the hydrogen burner is communicated with a hydrogen main pipe. In the present application, the hydrogen burner is located above the combustion chamber, and the high-temperature gas generated by combustion is pushed from top to bottom by air pressure and discharged from the air outlet at the lower part. Driven by the wind pressure, the high-temperature gas resists its own upward trend, so that the high-temperature gas can stay in the combustion chamber for a longer time, making closer and longer contact with the heated evaporator, methanol evaporator, medium-temperature heater and condenser in the combustion chamber. The retention of the high-temperature gas can significantly improve the heat transfer efficiency between the high-temperature gas and the heated components, enabling the heat to be fully conducted, greatly saving energy, avoiding the discharge of the heat carried by the high-temperature gas without being fully absorbed, and enabling the energy to be utilized to the fullest extent, thereby reducing the fuel cost. Moreover, due to the longer retention time of the high-temperature gas in contact with the heated components in this reverse combustion structure, the size of the heated components can be significantly reduced. A smaller size of the heated components can achieve the purpose of fully absorbing the heat of the gas, and it can be realized without a huge heating structure, thus saving the manufacturing cost.
[0006] In the present application, the methanol-to-hydrogen co-combustion evaporator can be used in coordination with a methanol-to-hydrogen production device. The residual temperature of the high-temperature gas in this device after generating water vapor is sufficient to vaporize methanol and make the methanol vapor in the optimal temperature range for catalytic hydrogen production and can be directly used for the catalytic reaction of methanol-to-hydrogen production. After the methanol vapor enters the methanol-to-hydrogen production device, it can maintain stable and efficient hydrogen production without the need for an additional heating device. The two have the beneficial effects of good synergistic efficiency, reduced energy consumption, and reduced use and maintenance costs.
[0007] As a preferred solution, the hydrogen burner includes a hydrogen pipe and a flame nozzle. The flame nozzle is arranged on the hydrogen pipe and faces the evaporator below. There is a high-temperature combustion chamber between the flame nozzle and the evaporator. The traveling direction of the high-temperature gas in the hydrogen fuel evaporation device is completely different from that of a traditional burner. In this application, the high-temperature gas is forced to circulate from top to bottom by a blower. Under the action of the upward driving force of the high-temperature gas, the high-temperature gas is driven by the blower to travel from top to bottom, so that it can better come into close contact with the evaporator, methanol evaporator, medium-temperature heater and condenser below. At the same time, the residence time of the high-temperature gas in the combustion chamber is increased, greatly increasing the heat transfer efficiency between the two, thereby improving the energy use efficiency, reducing heat waste and saving the use cost.
[0008] As a preferred solution, a firewall is provided on the inner wall of the combustion chamber. The firewall extends downward from the high-temperature combustion chamber to the medium-temperature heater. The firewall is made of high-temperature resistant material to prevent the combustion chamber from being damaged by high temperature.
[0009] As a preferred solution, both the evaporator and the medium-temperature heater are formed by coiling boiler tubes. Heat-conducting fins are arranged on the outer periphery of the boiler tubes. The boiler tubes are coiled to form a staggered multi-layer and one-layer multi-row distribution structure. One-layer multi-row means that the boiler tubes at the same height are arranged side by side or spirally, and staggered multi-layer means that the adjacent boiler tubes between the upper and lower layers are staggered at intervals. The staggered multi-layer and one-layer multi-row distribution structure makes the high-temperature gas present a complex and slow discharge path, enabling it to come into more and longer close contact with the evaporator and the medium-temperature heater, generating good heat conduction, greatly optimizing the heat transfer and reducing heat leakage.
[0010] As a preferred solution, the methanol evaporator is formed by coiling methanol evaporation tubes. The methanol evaporation tubes are located in the gaps formed by the intersection of the boiler tubes that make up the evaporator and the medium-temperature heater. A flat-layer methanol evaporator formed by coiling methanol evaporation tubes is located between the evaporator and the medium-temperature heater and can obtain high-temperature conduction of the combustion flame. After the high temperature of the flame is absorbed by the evaporator, the remaining high temperature is sufficient to raise the temperature of the methanol in the methanol evaporator to the catalytic suitable temperature for methanol to hydrogen production. Therefore, after the entire system operates stably in a cycle, the heating tubes in the hydrogen production catalytic tank can completely stop electric heating and rely entirely on the high temperature of methanol vapor to maintain hydrogen production. After the high-temperature gas heats and vaporizes methanol, the high-temperature gas further absorbs heat through the medium-temperature heater, and its remaining heat is already less and will not have an adverse impact on the outer shell of the combustion chamber. After further absorbing heat in the condenser at a lower position, it can be directly discharged. Hydrogen combustion only produces a small amount of water vapor and there are no pollutants that need to be treated subsequently, so the equipment for subsequent pollution treatment is completely eliminated, and the investment and maintenance costs of environmental protection equipment are completely cancelled, greatly reducing the overall use cost of steam.
[0011] Due to the adoption of the above technical solution, compared with the prior art, the advantages of the present invention are as follows:
[0012] The present invention discloses a methanol-to-hydrogen synergistic hydrogen combustion evaporator, which adopts a hydrogen fuel evaporation device. In the hydrogen fuel evaporation device, while steam is generated by hydrogen combustion, methanol vapor is also generated. The high-temperature methanol vapor can directly enter the methanol-to-hydrogen device, and its own temperature can fully maintain the operation of the methanol catalytic hydrogen production system. The hydrogen generated by this system enters the hydrogen fuel evaporation device to maintain the production of industrial steam and methanol vapor. The hydrogen burner of this application adopts reverse combustion technology, which significantly increases the residence time of the high-temperature combustion gas generated by combustion in the combustion chamber, and then greatly increases the heat transfer efficiency of the high-temperature combustion gas to the heated components. It not only significantly reduces the overall energy consumption and improves the thermal efficiency, but also makes the substances discharged from the entire system only water vapor, completely eliminating the need for other environmental protection waste treatment equipment, greatly reducing the equipment investment, and also significantly reducing the operation and maintenance costs of the equipment.
[0013] The following further illustrates the present invention in conjunction with the drawings and specific embodiments. BRIEF DESCRIPTION OF THE DRAWINGS
[0014] FIG. Figure 1 is a schematic diagram of the overall structure of the methanol-to-hydrogen synergistic hydrogen combustion evaporator of the present invention.
[0015] FIG. Figure 2 is a schematic diagram of the structure of the air chamber and the combustion chamber of the methanol-to-hydrogen synergistic hydrogen combustion evaporator of the present invention.
[0016] FIG. Figure 3 is a schematic diagram of the structure of the air chamber and the combustion chamber of the methanol-to-hydrogen synergistic hydrogen combustion evaporator of the present invention from another perspective after being cut open.
[0017] In the drawings: 1. Air chamber; 2. Combustion chamber; 3. Hydrogen burner; 31. Hydrogen pipe; 32. Flame nozzle; 4. Evaporator; 5. Methanol evaporator; 6. Medium-temperature heater; 7. Condenser; 8. Methanol pump; 9. Methanol storage tank; 10. Fan; 11. Water pump; 12. High-temperature combustion chamber; 13. Firewall; 14. Hydrogen main pipe. DETAILED DESCRIPTION OF THE EMBODIMENTS
[0018] Example: As Figures 1 to 3As shown in the figure, the methanol-to-hydrogen co-combustion evaporator includes an air chamber 1 and a combustion chamber 2. The air chamber 1 is connected to a blower 10 through a pipeline. The lower part of the air chamber 1 communicates with the upper part of the combustion chamber 2. The lower part of the combustion chamber 2 is provided with an air outlet. Inside the combustion chamber 2, a hydrogen burner 3, an evaporator 4, a methanol evaporator 5, a medium-temperature heater 6, and a condenser 7 are arranged in sequence from top to bottom. The hydrogen burner 3 is arranged between the air chamber 1 and the combustion chamber 2, and the combustion direction of the hydrogen burner 3 faces the evaporator 4 below. The water inlet end of the condenser 7 is connected to a water pump 11, the water outlet end of the condenser 7 communicates with the water inlet end of the medium-temperature heater 6, the water outlet end of the medium-temperature heater 6 communicates with the water inlet end of the evaporator 4, the liquid inlet end of the methanol evaporator 5 is connected to a methanol storage tank 9 through a methanol pump 8, and the liquid outlet end of the methanol evaporator 5 is connected to a methanol vapor pipe, which can be connected to the methanol vapor input port of the methanol-to-hydrogen catalytic device to provide methanol vapor with a suitable catalytic hydrogen production reaction temperature for the methanol-to-hydrogen catalytic device, reducing or eliminating the part of heating methanol to steam in methanol-to-hydrogen production. The air inlet end of the hydrogen burner 3 is connected to a hydrogen main pipe 14, and through the hydrogen main pipe 14, it can be connected to the hydrogen output pipe of the methanol-to-hydrogen catalytic device, directly using the methanol produced by the methanol-to-hydrogen device for the burner. Of course, the burner in this application can also be directly used for external hydrogen supply.
[0019] As shown in the attached Figure 2 and Figure 3 figure, the hydrogen burner 3 includes a hydrogen pipe 31 and a flame nozzle 32. The flame nozzle 32 is arranged on the hydrogen pipe 31 and faces the evaporator 4 below. There is a high-temperature combustion chamber 12 between the flame nozzle 32 and the evaporator 4. The traveling direction of the high-temperature gas of the hydrogen fuel evaporation device is completely different from that of the traditional burner. In this application, the high-temperature gas is forced to circulate from top to bottom by the blower. Under the action of the upward driving force of the high-temperature gas, the high-temperature gas is driven by the blower to travel from top to bottom, so that it can better come into close contact with the evaporator, methanol evaporator, medium-temperature heater, and condenser below, greatly increasing the heat transfer efficiency between the two, thereby improving the energy use efficiency, reducing heat waste, and saving the use cost.
[0020] As shown in the attached Figure 3 figure, a firewall 13 is provided on the inner wall of the combustion chamber 2. The firewall 13 extends downward from the high-temperature combustion chamber 12 to the medium-temperature heater 6.
[0021] In this embodiment, both the evaporator 4 and the medium-temperature heater 6 are formed by coiling boiler tubes. Heat-conducting fins are arranged on the outer periphery of the boiler tubes. The boiler tubes are coiled to form a staggered multi-layer and one-layer multi-row distribution structure. One-layer multi-row means that the boiler tubes at the same height are arranged side by side or spirally, and staggered multi-layer means that the adjacent boiler tubes between the upper and lower layers are staggered at intervals.
[0022] As shown in the attachedFigure 2 and 3 As shown, the methanol evaporator 5 is formed by coiling methanol evaporation tubes, and the methanol evaporation tubes are located between the gaps formed by the staggered boiler tubes of the evaporator 4 and the medium-temperature heater 6. A flat-layer methanol evaporator formed by coiling methanol evaporation tubes is located between the evaporator 4 and the medium-temperature heater 6, and can obtain the high-temperature conduction of the combustion flame. After the high temperature of the flame is absorbed by the evaporator, the remaining high temperature is sufficient to raise the temperature of the methanol inside the methanol evaporator to the catalytic suitable temperature for methanol hydrogen production. Therefore, after the entire system operates stably in circulation, the heating tubes in the hydrogen production catalytic tank can completely stop electric heating and rely entirely on the high temperature of methanol vapor to maintain hydrogen production. After the high-temperature gas heats and vaporizes methanol, the high-temperature gas further absorbs heat through the medium-temperature heater, and its remaining heat is already less and will not have an adverse impact on the outer shell of the evaporation device. After further absorbing heat in the condenser at a lower position, it can be directly discharged. Hydrogen combustion only produces a small amount of water vapor and there are no pollutants that need to be treated subsequently, so the equipment for subsequent pollution treatment is completely eliminated, and the investment and maintenance costs of environmental protection equipment are completely cancelled, greatly reducing the overall use cost of steam.
[0023] The methanol hydrogen production collaborative hydrogen combustion evaporator of the present application uses hydrogen as fuel and starts quickly. It only takes 3 minutes to start from cold state to maintain normal steam output in the whole system. The steam output of the system can reach one ton per hour. Only 70 kg of methanol is required for the supporting methanol hydrogen production equipment. Calculated at the current market price of methanol of 2.2 yuan per kg, the cost is only 11 yuan. In comparison, for the currently most common natural gas boiler and coal-fired boiler, their startup speeds are both measured in hours, far lower than the startup speed of several minutes of the present application. The natural gas consumption of the natural gas boiler for one ton of steam is 75 cubic meters, and the cost calculated at the current price of 4 yuan per cubic meter is 300 yuan per ton of steam. The coal consumption of the coal-fired boiler is 8 kg, and the cost calculated at the current price of 1.2 yuan per kg is 60 yuan per ton of steam. Comparing the two, the fuel use cost of the present application is the lowest and the startup speed is the fastest. Another great advantage of the present application is environmental protection. The steam of the present application is generated by hydrogen combustion. Hydrogen combustion only produces water and there are no pollutants that need to be treated, so there is no need for subsequent waste gas treatment, which is far superior to natural gas boilers and coal-fired boilers. The latter two will produce air pollutants and both require a certain amount of purification treatment, and environmental protection expenditures are also required. The present application completely eliminates this part of the expenditure.
[0024] In addition, the height and width of the evaporator in the present application are 229*480 mm. Compared with coal-fired boilers with the same output, the floor area is only 1 / 3 of theirs, which can greatly save the installation area and improve the site use efficiency.
Claims
1. A methanol-to-hydrogen evaporator with hydrogen combustion, comprising a wind chamber and a combustion chamber, characterized in that: The lower part of the wind chamber is communicated with the upper part of the combustion chamber, and the lower part of the combustion chamber is provided with an air outlet. A hydrogen burner, an evaporator, a methanol evaporator, a medium-temperature heater and a condenser are arranged in the combustion chamber from top to bottom. The hydrogen burner is arranged between the wind chamber and the combustion chamber, and the combustion direction of the hydrogen burner is toward the evaporator below. The water inlet end of the condenser is connected to a water pump, and the water outlet end of the condenser is communicated with the water inlet end of the medium-temperature heater, and the water outlet end of the medium-temperature heater is communicated with the water inlet end of the evaporator. The liquid inlet end of the methanol evaporator is communicated with the methanol storage tank through a methanol pump, and the liquid outlet end of the methanol evaporator is connected to a methanol steam pipe. The air inlet end of the hydrogen burner is connected to a hydrogen main pipe.
2. The methanol-to-hydrogen assisted hydrogen combustion evaporator according to claim 1 is characterized in that: The hydrogen burner comprises a hydrogen pipe and a flame nozzle. The flame nozzle is arranged on the hydrogen pipe and faces the evaporator below. A high-temperature combustion chamber is provided between the flame nozzle and the evaporator.
3. The methanol-to-hydrogen assisted hydrogen combustion evaporator according to claim 2 is characterized in that: The inner wall of the combustion chamber is provided with a fire wall, and the fire wall extends downward from the high-temperature combustion chamber to the medium-temperature heater.
4. The methanol-to-hydrogen assisted hydrogen combustion evaporator according to any one of claims 1 to 3, characterized in that: The evaporator and the medium-temperature heater are both composed of coiled boiler tubes. The outer circumference of the boiler tubes is provided with heat-conducting fins. The boiler tubes are coiled to form staggered multi-layer and multi-row distribution structures. The multi-row structure is composed of boiler tubes of the same height arranged side by side or spirally arranged, and the staggered multi-layer structure is composed of adjacent boiler tubes between the upper and lower layers at staggered intervals.
5. The methanol-to-hydrogen assisted hydrogen combustion evaporator according to claim 4 is characterized in that: The methanol evaporator is formed by winding methanol evaporation tubes, and the methanol evaporation tubes are located between the gaps formed by the boiler tubes constituting the evaporator and the medium-temperature heater.