CN215516649U - Natural gas hydrogen production device - Google Patents
Natural gas hydrogen production device Download PDFInfo
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- CN215516649U CN215516649U CN202122014833.1U CN202122014833U CN215516649U CN 215516649 U CN215516649 U CN 215516649U CN 202122014833 U CN202122014833 U CN 202122014833U CN 215516649 U CN215516649 U CN 215516649U
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Abstract
The utility model discloses a natural gas hydrogen production device which comprises a natural gas buffer tank, a reforming furnace, a phosphoric acid dosing device, a deaerator, a shift converter, a heat exchanger, a water cooler, a reforming gas separator, a reforming gas buffer tank, a pressure swing adsorption mechanism and a hydrogen buffer tank, wherein the natural gas buffer tank, the reforming furnace, the phosphoric acid dosing device, the deaerator, the shift converter, the heat exchanger, the water cooler, the reforming gas separator, the reforming gas buffer tank, the pressure swing adsorption mechanism and the hydrogen buffer tank are sequentially connected through a pipeline, the pressure swing adsorption mechanism comprises a plurality of adsorption towers, and the adsorption towers are connected in parallel. The utility model realizes the production of hydrogen by using natural gas, the reformer is set as a top-burning cylinder furnace, the convection section heat exchange coil is simplified as much as possible, and the failure rate and the maintenance workload of the device are reduced.
Description
Technical Field
The utility model relates to the technical field of hydrogen production, in particular to a natural gas hydrogen production device.
Background
The method is characterized in that light hydrocarbons (natural gas, decarbonized biogas, light naphtha and dry gas) are used as raw materials to prepare industrial hydrogen, a steam conversion process and an autothermal conversion process are adopted, the process of reforming and making gas (SMR) by natural gas steam and pressure swing adsorption purification and separation to extract hydrogen (PSA) is adopted from the aspects of safety, long-period stable operation and the current industrial equipment manufacturing level and investment cost, the existing hydrogen production device is poor in stability, and when one link of the whole device breaks down, the whole device stops working, the production progress is influenced, and potential safety hazards are caused.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a natural gas hydrogen production device to solve the problems in the background technology.
In order to achieve the purpose, the utility model provides the following technical scheme: the natural gas buffer tank, the reforming furnace, the phosphoric acid dosing device, the deaerator, the heat exchanger, the water cooler, the reforming gas separator, the reforming gas buffer tank, the pressure swing adsorption mechanism and the hydrogen buffer tank are sequentially connected through a pipeline, the pressure swing adsorption mechanism comprises a plurality of adsorption towers, and the adsorption towers are connected in parallel.
Preferably, the reformer is of a top-firing barrel furnace structure, and the specific structure is that a downward burner is arranged at the center of a barrel, and a furnace tube is arranged at the radial periphery of the burner.
Preferably, the tail gas output port of the reformer is further connected with an induced draft fan, the induced draft fan is connected with a chimney, and the tail gas is absorbed by the induced draft fan and then discharged from the chimney.
Preferably, the tail end of the reformer is further connected with an air blower which blows air into the reformer, so that the combustion is more sufficient.
Preferably, a desorption gas buffer tank is arranged between the pressure swing adsorption mechanism and the hydrogen buffer tank, so that the defects of large flow and pressure fluctuation and low combustion efficiency of a radiation section of the reforming furnace when the pressure swing adsorption desorption gas is used as the fuel of the reforming furnace are overcome, and the combustion operation of the reforming furnace is stabilized by effectively controlling the flow of the flushing gas.
Preferably, a reformed gas waste heat boiler is arranged between the reforming furnace and the intermediate converter and is used for recovering the waste heat of the mixed gas discharged from the reforming furnace.
The utility model has the following beneficial effects: the natural gas hydrogen production device comprises a natural gas buffer tank, a reforming furnace, a phosphoric acid dosing device, a deaerator, a variable-pressure furnace, a heat exchanger, a water cooler, a reforming gas separator, a reforming gas buffer tank, a pressure swing adsorption mechanism and a hydrogen buffer tank, the natural gas hydrogen production device is used for producing hydrogen by using natural gas, the reforming furnace is arranged as a top-fired cylindrical furnace, a convection section heat exchange coil is simplified as much as possible, and the failure rate and the maintenance workload of the device are reduced.
In order to make the aforementioned and other objects, features and advantages of the utility model comprehensible, preferred embodiments accompanied with figures are described in detail below.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view showing the connection relationship of a natural gas surge tank according to the present invention;
FIG. 2 is a schematic view showing the connection relationship of the reformer according to the present invention;
FIG. 3 is a schematic view showing the connection relationship of the phosphoric acid adding device according to the present invention;
FIG. 4 is a schematic view showing the connection relationship of the hydrogen buffer tank according to the present invention;
fig. 5 is a schematic flow chart of the present invention.
Reference numerals of the above figures: the system comprises a natural gas buffer tank 10, a reformer 11, a phosphoric acid dosing device 12, a deaerator 13, a shift converter 14, a heat exchanger 15, a water cooler 16, a reforming gas separator 17, a reforming gas buffer tank 18, a pressure swing adsorption mechanism 19, an adsorption tower 191, a hydrogen buffer tank 20, an induced draft fan 21, a chimney 22, an air blower 23 and a desorption gas buffer tank 24.
Detailed Description
The technical solutions in the embodiments of the present invention will be described below in detail and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Referring to fig. 1-5, a natural gas hydrogen production device comprises a natural gas buffer tank 10, a reformer 11, a phosphoric acid dosing device 12, a deaerator 13, a converter 14, a heat exchanger 15, a water cooler 16, a reforming gas separator 17, a reforming gas buffer tank 18, a pressure swing adsorption mechanism 19 and a hydrogen buffer tank 20, wherein the natural gas buffer tank 10, the reformer 11, the phosphoric acid dosing device 12, the deaerator 13, the converter 14, the heat exchanger 15, the water cooler 16, the reforming gas separator 17, the reforming gas buffer tank 18, the pressure swing adsorption mechanism 19 and the hydrogen buffer tank 20 are sequentially connected through a pipeline, the pressure swing adsorption mechanism 19 comprises a plurality of adsorption towers 191, and the adsorption towers 191 are connected in parallel.
Furthermore, the reformer 11 is a top-fired cylindrical furnace structure, and the specific structure is that a downward burner is arranged at the center of a cylindrical barrel, a furnace tube is arranged at the radial periphery of the burner, and the peripheral furnace tube is heated by the burner, so that accidents in the operation of the traditional reformer, the failure of the furnace tube and the failure of the hydrogen production device can be avoided, and the reformer can strengthen the operation mode of the reformer by cutting the failed furnace tube, thereby achieving the purpose of continuously outputting hydrogen.
Further, the tail gas output port of the reformer 11 is further connected with an induced draft fan 21, the induced draft fan 21 is connected with a chimney 22, and the tail gas is absorbed by the induced draft fan 21 and then discharged from the chimney 22.
Further, an air blower 23 is connected to the tail end of the reformer 11 to blow air into the reformer 11, so that combustion is more complete.
Further, a desorption gas buffer tank 24 is arranged between the pressure swing adsorption mechanism 19 and the hydrogen gas buffer tank 20, the defects that when the pressure swing adsorption desorption gas is used as the fuel of the reformer, the flow and pressure fluctuation are large, and the combustion efficiency of the radiation section of the reformer is low are overcome, the combustion operation of the reformer is stabilized by effectively controlling the flow of the flushing gas, the pressure swing adsorption consists of 5 adsorption towers, 1 adsorption tower is in an adsorption state at any moment, components such as methane, carbon dioxide and carbon monoxide in the reforming gas are stopped on the surface of the adsorbent, and hydrogen is collected from the top of the adsorption tower as a non-adsorption component and is sent to the outside. The adsorbent saturated with the impurity components is desorbed from the adsorbent through a regeneration step, and is sent to a converter as fuel after being collected. The regeneration step of the adsorption tower comprises 10 steps of uniform descending, sequential releasing, reverse releasing, flushing, uniform ascending, final ascending and the like, after regeneration is finished, the adsorption tower has the capacity of treating converted gas and producing hydrogen again, and the steps are carried out by 5 adsorption tower streams to ensure the purposes of continuously treating the converted gas and continuously producing the hydrogen simultaneously.
Further, a reformed gas waste heat boiler is arranged between the reforming furnace 11 and the intermediate converter 14 and is used for recovering the mixed gas waste heat from the reforming furnace 11.
The specific working flow is as follows, referring to fig. 5, after passing through a natural gas separator, natural gas outside a battery compartment is partially and directly sent to a reformer fuel system, most of the natural gas enters a natural gas compressor, is pressurized to 1.6MPaA, is heated to about 380 ℃ by a feed gas preheater of a convection section of a steam reformer, enters a desulfurizer, is used for removing sulfur in the feed gas to below 0.2PPM, the desulfurized feed gas and process steam (1.8 MPaA) are subjected to automatic value adjustment of mixed gas preheater according to H2O/sigma C = 3-4, is further preheated to above 500 ℃, and uniformly enters a reformer from an upper gas collecting main pipe and an upper pig tail pipe, and reacts with water steam to generate CO and H2 in a catalyst layer, heat required for hydrocarbon conversion is provided by burning fuel mixed gas by a top burner, the temperature of the reformer is-800 ℃, the residual methane content is about-4.0%, and high-temperature converted gas enters a pipe pass of a boiler, generating saturated steam of 1.8MPaA, reducing the temperature of converted gas discharged from a waste heat boiler to 360 ℃, entering a middle-pressure gas converting furnace for medium-temperature conversion reaction, further generating hydrogen from CO, wherein the content of CO in the gas discharged from the converting furnace is less than 2%, sequentially entering the middle-pressure gas converting furnace heat exchanger, a boiler feed water preheater and a desalted water preheater for heat recovery, cooling to 40 ℃ by a converted gas water cooler, separating the process condensate from the middle-pressure gas by a process gas of a water outlet cooler through a separator, and sending the process gas to pressure swing adsorption. The fuel gas is mixed with the desorption gas of pressure swing adsorption before entering the bottom burner, and then the fuel gas quantity is adjusted according to the temperature of the gas at the outlet of the reformer. The fuel gas enters the top burner for burning after the flow is regulated, and provides heat for the reformer.
The working principle is as follows: after passing through a natural gas separator, a small part of natural gas outside a battery compartment is directly sent to a reformer fuel system, the majority of the natural gas enters a natural gas compressor, is boosted to 1.6MPaA, is heated to about 380 ℃ by a feed gas preheater of a convection section of a steam reformer, enters a desulfurizer, is desulfurized in the desulfurizer to remove sulfur in the feed gas to below 0.2PPM, the desulfurized feed gas and process steam (1.8 MPaA) are subjected to automatic value adjustment of a mixed gas preheater according to H2O/sigma C = 3-4, is further preheated to above 500 ℃, uniformly enter a reformer from an upper gas collecting main pipe and an upper pig tail pipe, react with water vapor to generate CO and H2 in a catalyst layer, heat required by hydrocarbon conversion is provided by a fuel mixed gas burning nozzle at the top, the temperature of the gas exiting the reformer is-800 ℃, the content of residual methane is about-4.0%, and the high-temperature converted gas enters the tube pass of a boiler, generating 1.8MPaA saturated steam, reducing the temperature of the converted gas out of the waste heat boiler to 360 ℃, and entering the medium temperature shift reaction of the medium temperature shift furnace to further generate hydrogen from CO. The CO content in the gas out of the shift converter is less than 2 percent, the medium shift gas enters a medium shift gas heat exchanger, a boiler feed water preheater and a desalted water preheater in sequence to recover heat, then is cooled to 40 ℃ by a converted gas water cooler, the process gas out of a water cooler passes through a separator to separate process condensate from the medium shift gas, the process gas is sent to pressure swing adsorption, the fuel gas is mixed with desorption gas of the pressure swing adsorption before entering a bottom burner, the fuel gas flow is adjusted according to the temperature of the gas at the outlet of the shift converter, the fuel gas enters a top burner to be combusted after flow adjustment, heat is provided for the shift converter to recover the heat of the flue gas, four groups of heat exchange coil pipes are arranged in a convection section of the converter, the process condensate which is separated by the conversion gas separator and contains dissolved gases such as CO2, H2 and the like is sent to a sewage treatment station after pressure reduction, the pressure of the desalted water outside a boundary area is about 0.3MPaA, and residual oxygen is removed in a deoxygenation tank, the deoxidized water is pressurized by a boiler water feeding pump and then enters a boiler water feeding preheater of a conversion process, the preheated deoxidized water is sent to a waste boiler, and a small amount of phosphate solution is added into the deoxidized water which is discharged from a deoxidized tank so as to improve the scaling condition of the boiler water. The drum needs to continuously discharge part of boiler water to control the total dissolved solid amount of the boiler water in the drum.
Finally, it should be noted that: although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that changes may be made in the embodiments and/or equivalents thereof without departing from the spirit and scope of the utility model. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention shall be included in the contents of the present invention within the scope of the protection of the present invention.
Claims (6)
1. The utility model provides a natural gas hydrogen plant, includes natural gas buffer tank (10), reborner (11), phosphoric acid charge device (12), oxygen-eliminating device (13), well stove (14), heat exchanger (15), water cooler (16), conversion gas separator (17), conversion gas buffer tank (18), pressure swing adsorption mechanism (19) and hydrogen buffer tank (20), its characterized in that: the natural gas buffer tank (10), the reforming furnace (11), the phosphoric acid dosing device (12), the deaerator (13), the shift converter (14), the heat exchanger (15), the water cooler (16), the reforming gas separator (17), the reforming gas buffer tank (18), the pressure swing adsorption mechanism (19) and the hydrogen buffer tank (20) are sequentially connected through a pipeline, the pressure swing adsorption mechanism (19) comprises a plurality of adsorption towers (191), and the adsorption towers (191) are connected in parallel.
2. A natural gas hydrogen plant according to claim 1, characterized in that: the reforming furnace (11) is of a top-burning barrel furnace structure, the specific structure is that a downward burning nozzle is arranged at the center of a barrel, and a furnace tube is arranged at the radial periphery of the burning nozzle.
3. A natural gas hydrogen plant according to claim 1, characterized in that: the tail gas output port of the reformer (11) is further connected with an induced draft fan (21), the induced draft fan (21) is connected with a chimney (22), and the tail gas is absorbed by the induced draft fan (21) and then discharged from the chimney (22).
4. A natural gas hydrogen plant according to claim 1, characterized in that: the tail end of the reformer (11) is also connected with an air blower (23) which is blown into the reformer (11) through air, so that the combustion is more complete.
5. A natural gas hydrogen plant according to claim 1, characterized in that: a desorption gas buffer tank (24) is arranged between the pressure swing adsorption mechanism (19) and the hydrogen buffer tank (20), the defects of large flow and pressure fluctuation and low combustion efficiency of a radiation section of the reforming furnace when pressure swing adsorption desorption gas is used as fuel of the reforming furnace are overcome, and the combustion operation of the reforming furnace is stabilized by effectively controlling the flow of flushing gas.
6. A natural gas hydrogen plant according to claim 1, characterized in that: a reformed gas waste heat boiler is arranged between the reforming furnace (11) and the intermediate transformer furnace (14) and is used for recovering the mixed gas waste heat coming out of the reforming furnace (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122014833.1U CN215516649U (en) | 2021-08-25 | 2021-08-25 | Natural gas hydrogen production device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202122014833.1U CN215516649U (en) | 2021-08-25 | 2021-08-25 | Natural gas hydrogen production device |
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| CN215516649U true CN215516649U (en) | 2022-01-14 |
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| CN202122014833.1U Active CN215516649U (en) | 2021-08-25 | 2021-08-25 | Natural gas hydrogen production device |
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2021
- 2021-08-25 CN CN202122014833.1U patent/CN215516649U/en active Active
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