CN212864131U

CN212864131U - Heat-conducting oil-free methanol hydrogen production device

Info

Publication number: CN212864131U
Application number: CN202021798044.0U
Authority: CN
Inventors: 王均衡; 王海东
Original assignee: Individual
Current assignee: Foshan Yiwei Technology Co ltd
Priority date: 2020-08-25
Filing date: 2020-08-25
Publication date: 2021-04-02
Anticipated expiration: 2030-08-25

Abstract

The utility model relates to a hydrogen preparation technical field specifically discloses a methanol hydrogen production device of exempting from conduction oil, including the heat accumulator, vaporization overheat coil pipe and with the light-wave tube of heat accumulator intercommunication, be equipped with gas outlet and air inlet on the heat accumulator, be equipped with vaporizing tube and superheater in the vaporization overheat coil pipe, the gas outlet of heat accumulator and the superheater intercommunication in the vaporization overheat coil pipe, the air inlet department intercommunication of vaporizing overheat coil pipe's vaporizing tube has the liquid feed pump, vaporizing overheat coil pipe's vaporizing tube gas outlet department intercommunication has the cracker, the intercommunication has the buffer tank on the cracker, the intercommunication has the spark arrester on the buffer tank, the back-fire relief end intercommunication of spark arrester has the hydrogen burner, the intercommunication has the function tube dish on the steam diffusion tube of hydrogen burner, the other end of function tube dish and the air inlet intercommunication of heat accumulator.

Description

Heat-conducting oil-free methanol hydrogen production device

Technical Field

The utility model relates to a hydrogen preparation technical field specifically discloses a methanol hydrogen production device of exempting from conduction oil.

Background

The hydrogen production from methanol refers to a process of mixing methanol and water vapor, and then subjecting the mixture to the action of a catalyst under certain temperature and pressure conditions to cause the methanol to undergo a cracking reaction and finally obtain hydrogen and carbon dioxide. The main chemical reaction formula of reforming methanol and steam is as follows:

CH_3OH→CO+2H2(1)；CH_3OH→CO+(1)+H2(2)；CH_3OH+H_2O→CO2+3H2(3)

the methanol-to-hydrogen method in industry is characterized by that the methanol and desalted water are mixed according to a certain proportion, then fed into vaporization tower to make vaporization, the vaporized water-methanol steam is passed through superheater and superheated, then fed into converter, the catalyst is placed in the converter, and the water-methanol steam is undergone the action of catalyst to make cracking reaction in the converter to produce hydrogen gas and carbon dioxide.

The main defects of the methanol hydrogen production equipment in the prior art are as follows: 1. the whole equipment is large and complex, and the manufacturing cost is high; 2. the heat conduction oil used for providing a heat source for the superheater and the converter is heated by a stainless steel thermocouple, so that the heat conduction oil has uneven heating area, large power consumption, fouling resistance and short service life; 3. a pressure container needs to be built, and the pipe arrangement in the container is complex in construction, long in construction period, time-consuming and labor-consuming; 4. a large amount of heat conducting oil is generally filled in the shell pass of the pressure container, and the heat conducting oil is used for vaporizing mixed gas entering an additive in a heat exchange cracking tube, and directly vaporizing and cracking the mixed gas to convert the mixed gas into hydrogen, so that the heat conducting oil-free methanol hydrogen production device is provided, and the problems are solved.

SUMMERY OF THE UTILITY MODEL

The utility model aims to solve the problem of large power consumption of the traditional hydrogen production equipment.

In order to achieve the purpose, the utility model discloses a basic scheme provides a methanol hydrogen production device of exempting from conduction oil, including heat accumulator, vaporization overheat coil pipe and the light wave tube that communicates with the heat accumulator, be equipped with gas outlet and air inlet on the heat accumulator, be equipped with vaporizing tube and superheater tube in the vaporization overheat coil pipe, the gas outlet of heat accumulator communicates with the superheater tube in the vaporization overheat coil pipe, the air inlet department of vaporizing tube of vaporization overheat coil pipe communicates with the liquid feed pump, the vaporizer tube gas outlet department of vaporization overheat coil pipe communicates with the cracker;

the cracker is communicated with a buffer tank, the buffer tank is communicated with a flame arrester, the flame arresting end of the flame arrester is communicated with a hydrogen burner, the hot gas diffusion pipe of the hydrogen burner is communicated with a functional pipe disc, and the other end of the functional pipe disc is communicated with the air inlet of the heat accumulator.

The principle and effect of this basic scheme lie in:

1. the method is characterized in that a light wave tube is firstly utilized for heating, in the heating process, one part of heat is input into a production empty space for production, the other part of heat enters a heat accumulator for heating, the tradition that a heat conduction furnace heating circulation system cannot be opened is omitted, a vaporization tank and a cracking tank are omitted, a tail gas waste heat coil pipe is adopted for vaporization and cracking to prepare hydrogen, and the special chemical engineering design institute is not needed for one-by-one design, so that the production and the use can be realized.

2. When the light wave tube heats the heat accumulator to a certain temperature, the power supply of the light wave tube can be turned off, the heat accumulator begins to deliver the stored heat to the overheating pipe of the vaporization overheating coil, the heat in the overheating pipe of the vaporization overheating coil is transferred to the gasification pipe of the vaporization overheating coil through heat, the mixed liquid of methanol and water is delivered to the gasification pipe of the vaporization overheating coil, and the mixed liquid of the methanol and the water can be gasified by heating.

3. The mixed liquid of the gasified methanol and the water then enters the cracker with the catalyst along with the subsequent pressure, the mixed liquid of the gasified methanol and the water is converted into hydrogen in the cracker, and the hydrogen enters the buffer tank through the continuous pressure to wait for the subsequent use.

4. The hydrogen stored in the buffer tank enters the hydrogen burner through the flame arrester, the hydrogen burner burns to generate heat to enter the functional pipe coil, the functional pipe coil can be used by related users such as heating, drying, steam and fire ploughing, meanwhile, the heat used is stored in the heat accumulator, and the heat source is continuously provided for the vaporization overheating coil, so that the cyclic utilization of the waste heat is achieved.

Compared with the prior art, the methanol hydrogen production device avoids the problem of high power consumption, utilizes the waste heat generated after hydrogen energy is combusted to vaporize and carry out overheat cracking conversion to produce hydrogen, so that the mixed liquid of methanol and water is more environment-friendly, sanitary, economical and energy-saving to produce hydrogen, an environment-friendly road of energy conservation and emission reduction is provided for industrial methanol hydrogen production, and tail gas generated by the hydrogen production device is utilized to produce hydrogen circularly, thereby meeting the requirements of various industries on hydrogen energy.

Further, an air inlet valve and a pressure gauge for protecting the vaporization overheating coil are arranged between the liquid supply pump and the vaporization overheating coil. The pressure gauge can detect the pressure of vaporization, and the operation safety is guaranteed.

Further, the liquid supply pump is a metering pump with the flow controlled by the controller. The dosage of the mixed liquid of the methanol and the water can be controlled by using a metering pump according to the use requirement, so that the hydrogen output is controlled.

Further, a heat accumulator thermometer is arranged in the heat accumulator, and a hydrogen burner thermometer is arranged on the hydrogen burner. The hydrogen burner thermometer is provided with the stability in the heat accumulator, so that the temperature of the heat accumulator is controlled by adjusting the waste heat firepower of the burner, and the mixed liquid of vaporization, overheating and cracking hydrogen production is controlled to circulate in the heat accumulator.

Further, controlled valves are arranged between the vaporization overheating coil and the heat accumulator, between the vaporization overheating coil and the cracker, between the cracker and the buffer tank, between the flame arrester and the hydrogen combustion, and between the functional pipe coil and the heat accumulator. The controlled valve is convenient for controlling the running process of the whole device.

And the system further comprises a PLC (programmable logic controller), wherein the PLC is respectively and electrically connected with the air inlet valve, the pressure gauge, the metering pump, the heat accumulator thermometer, the hydrogen burner thermometer and the controlled valve. The PLC controller can be mapped according to the use requirement, and automatic control is realized.

Drawings

FIG. 1 is a front view of a heat-transfer oil-free methanol hydrogen production plant according to an embodiment of the present invention;

FIG. 2 is a partial cross-sectional view of a vaporization overheating coil in a heat transfer oil-free methanol hydrogen production plant according to an embodiment of the present invention;

fig. 3 is a flow chart of a methanol hydrogen production device without heat transfer oil according to an embodiment of the present invention.

Detailed Description

The following is further detailed by the specific embodiments:

reference numerals in the drawings of the specification include: the device comprises a heat accumulator 1, a light wave tube 2, a vaporization overheating coil 3, a mixed liquid inlet valve 4, a metering pump 5, a vaporization coil valve 6, a pressure gauge 7, a gas inlet valve 8, a cracker control valve 9, a cracker 10, a hydrogen roll-off valve 11, a buffer tube inlet valve 12, a buffer tank 13, a safety valve 14, a drain pipe 15, a drain valve 16, a mixed liquid outlet valve 17, a flame arrester 18, a control burner valve 19, a hydrogen burner 20, a functional coil 21, a circulation assembly 22, a flow pressure gauge 23, a circulation assembly valve 24, a distribution control cabinet 25, a hydrogen outlet valve 26, a hydrogen burner thermometer 27, a tail gas outlet chimney 28, a heat accumulator drain valve 29, a temperature gauge 30, a gasification tube 301 and a superheat tube 302.

A heat-conducting oil-free methanol hydrogen production device is disclosed, for example, a vaporizing tube 301 and a superheater tube 302 are arranged in a vaporizing and overheating coil 3 shown in FIG. 2, as shown in FIG. 1 and FIG. 3, the vaporizing and overheating coil 3 is installed on a heat accumulator 1, the heat accumulator 1 is provided with a tail gas outlet chimney 28 and a heat accumulator blow-down valve 29, an air outlet of the heat accumulator 1 is communicated with the superheater tube 302 in the vaporizing and overheating coil 3, a metering pump 5 is communicated with an air inlet of the vaporizing tube 301 of the vaporizing and overheating coil 3, a mixed liquid inlet valve 4 and a pressure gauge 7 for protecting the vaporizing and overheating coil 3 are arranged between the metering pump 5 and the vaporizing and overheating coil 3, the vaporizing tube 301 of the vaporizing and overheating coil 3 is further provided with an air inlet valve 8, a cracker 10 is communicated with the air outlet of the vaporizing and overheating coil 301 of the vaporizing and overheating coil 3, an air outlet of the cracker 10 is communicated with a, the buffer tank 13 is also communicated with a drain pipe 15 for draining and a mixed liquid outlet valve 17 for discharging mixed liquid of hydrogen and water, the drain pipe 15 is provided with a drain valve 16, the flame retarding end of the flame arrester 18 is communicated with the hydrogen burner 20, the hot gas diffusion pipe of the hydrogen burner 20 is communicated with a functional pipe disc 21, the other end of the functional pipe disc 21 is communicated with the air inlet of the heat accumulator 1, the heat accumulator 1 is internally provided with a heat accumulator thermometer 30, and the hydrogen burner 20 is provided with a hydrogen burner thermometer 27.

A vaporizing coil valve 6 is arranged between the vaporizing superheated coil 3 and the heat accumulator 1, a cracker control valve 9 is arranged between the vaporizing superheated coil 3 and the cracker 10, a hydrogen transfer valve 11 and a buffer tank inlet valve 12 are arranged between the cracker 10 and the buffer tank 13, a circulation component 22 and a flow pressure gauge 23 are also arranged between the cracker 10 and the buffer tank 13, the circulation component 22 comprises a water pump, an oil pump and a fan, a corresponding circulation component valve 24 is arranged on the circulation component 22, a safety valve 14 for pressure relief is arranged on the buffer tank 13, a control burner valve 19 is arranged between the flame arrester 18 and the hydrogen combustion, hydrogen outlet valves 26 are arranged between the functional coil 21 and the heat accumulator 1, and a PLC controller is respectively connected with the mixed liquid inlet valve 4, the vaporizing coil valve 6, the gas inlet valve 8, the cracker control valve 9, the hydrogen transfer valve 11, the buffer tank inlet valve 12, the hydrogen outlet valve 26, The safety valve 14, the blow-down valve 16, the mixed liquid outlet valve 17, the control burner valve 19, the circulation assembly 22, the flow pressure gauge 23, the circulation assembly valve 24, the hydrogen outlet valve 26, the pressure gauge 7, the metering pump 5, the heat accumulator thermometer 30 and the hydrogen burner thermometer 27 are electrically connected, and the PLC controller is installed in a power distribution control cabinet 25.

When putting into use, install this device in the assigned position, then communicate various conveying pipe, discharging pipe and blow off pipe 15 to, then this field technical personnel will control the program entry PLC controller of whole device, because this technical field technical personnel of control program simply can not belong to again the utility model discloses a protection object, so do not do too much the description here.

And starting the PLC control panel, starting the light wave tube 2 to heat to 250 ℃, starting the light wave tube 2 to heat to supply the users of all walks of life to work, simultaneously enabling a part of waste heat to enter the heat accumulator 1 and heat the heat accumulator 1, and cutting off the power supply of the light wave tube 2 by the PLC control panel after the temperature in the heat accumulator 1 rises to 250 ℃, so that the light wave tube 2 stops working.

The heat accumulator 1 starts to convey the stored heat to the overheating pipe 302 of the vaporization overheating coil 3, the heat in the overheating pipe 302 of the vaporization overheating coil 3 is transferred to the gasification pipe 301 of the vaporization overheating coil 3 through heat, the metering pump 5 is started, the installation and use requirements are met, the input quantity of the metering pump 5 is well controlled by the PLC, at the moment, the mixed liquid of methanol and water can be conveyed to the gasification pipe 301 of the vaporization overheating coil 3, and the mixed liquid of methanol and water can be gasified through heating.

The gasified mixed solution of methanol and water then enters the cracker 10 with the catalyst under subsequent pressure, the gasified mixed solution of methanol and water is converted into hydrogen in the cracker 10, and the hydrogen enters the buffer tank 13 under continuous pressure to wait for subsequent use.

The hydrogen stored in the buffer tank 13 enters the hydrogen burner 20 through the flame arrester 18, the hydrogen burner 20 burns to generate heat and enters the functional pipe coil 21, the functional pipe coil 21 can be used by related users such as heating, drying, steam and fire ploughing, meanwhile, the heat used is stored in the heat accumulator 1, and the heat source is continuously provided for the vaporization overheating coil 3, so that the recycling of waste heat is achieved.

The utility model discloses avoided the big problem of power consumption, utilized the waste heat after the hydrogen energy burning to come vaporization, overheated schizolysis conversion hydrogen manufacturing, made mixed liquid hydrogen manufacturing environmental protection health, economy, energy-conservation more of methanol and water, walked out an energy saving and emission reduction's environmental protection road for industry methyl alcohol hydrogen manufacturing, utilized the tail gas temperature circulation hydrogen manufacturing that hydrogen plant self produced to satisfy all walks each business to the hydrogen energy demand.

The above description is only for the embodiments of the present invention, and the common general knowledge of the known specific structures and characteristics in the schemes is not described herein too much, and those skilled in the art will know all the common technical knowledge in the technical field of the present invention before the application date or the priority date, can know all the prior art in this field, and have the ability to apply the conventional experimental means before this date, and those skilled in the art can combine their own ability to perfect and implement the schemes, and some typical known structures or known methods should not become obstacles for those skilled in the art to implement the present application. It should be noted that, for those skilled in the art, without departing from the structure of the present invention, several modifications and improvements can be made, which should also be regarded as the protection scope of the present invention, and these will not affect the effect of the implementation of the present invention and the practicability of the patent. The scope of the claims of the present application shall be determined by the contents of the claims, and the description of the embodiments and the like in the specification shall be used to explain the contents of the claims.

Claims

1. A methanol hydrogen production device free of heat conduction oil is characterized by comprising a heat accumulator, a vaporization overheating coil and a light wave tube communicated with the heat accumulator, wherein the heat accumulator is provided with an air outlet and an air inlet;

2. The heat-transfer oil-free methanol hydrogen production device according to claim 1, characterized in that: and an air inlet valve and a pressure gauge for protecting the vaporizing and overheating coil are arranged between the liquid supply pump and the vaporizing and overheating coil.

3. The heat-transfer oil-free methanol hydrogen production device according to claim 2 or the above, characterized in that: the liquid supply pump is a metering pump with the flow controlled by a controller.

4. The heat-transfer oil-free methanol hydrogen production device according to claim 3, characterized in that: and a heat accumulator thermometer is arranged in the heat accumulator, and a hydrogen burner thermometer is arranged on the hydrogen burner.

5. The heat-transfer oil-free methanol hydrogen production device according to claim 4, characterized in that: controlled valves are arranged between the vaporization overheating coil and the heat accumulator, between the vaporization overheating coil and the cracker, between the cracker and the buffer tank, between the flame arrester and the hydrogen combustion, and between the functional pipe coil and the heat accumulator.

6. The heat-transfer oil-free methanol hydrogen production device according to claim 5, characterized in that: the system also comprises a PLC controller which is respectively and electrically connected with the air inlet valve, the pressure gauge, the metering pump, the heat accumulator thermometer, the hydrogen burner thermometer and the controlled valve.