CN220425317U - Coal-to-methanol synthesis purge gas coupling high-purity hydrogen device - Google Patents
Coal-to-methanol synthesis purge gas coupling high-purity hydrogen device Download PDFInfo
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- CN220425317U CN220425317U CN202321961774.1U CN202321961774U CN220425317U CN 220425317 U CN220425317 U CN 220425317U CN 202321961774 U CN202321961774 U CN 202321961774U CN 220425317 U CN220425317 U CN 220425317U
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- 239000007789 gas Substances 0.000 title claims abstract description 156
- 239000001257 hydrogen Substances 0.000 title claims abstract description 145
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 145
- OKKJLVBELUTLKV-UHFFFAOYSA-N methanol Substances OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 141
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 135
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 50
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 50
- 238000010926 purge Methods 0.000 title claims abstract description 27
- 230000008878 coupling Effects 0.000 title claims abstract description 15
- 238000010168 coupling process Methods 0.000 title claims abstract description 15
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 15
- 238000001179 sorption measurement Methods 0.000 claims abstract description 35
- 239000002737 fuel gas Substances 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 16
- 230000001105 regulatory effect Effects 0.000 claims description 85
- 238000011084 recovery Methods 0.000 claims description 31
- 230000006835 compression Effects 0.000 claims description 13
- 238000007906 compression Methods 0.000 claims description 13
- 239000003245 coal Substances 0.000 claims description 10
- 230000000694 effects Effects 0.000 claims description 10
- 238000003795 desorption Methods 0.000 claims description 9
- 238000002309 gasification Methods 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 238000005406 washing Methods 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 abstract description 10
- 230000002093 peripheral effect Effects 0.000 abstract description 7
- 238000000034 method Methods 0.000 description 8
- 230000008569 process Effects 0.000 description 5
- 239000000446 fuel Substances 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000011070 membrane recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model relates to a coal-to-methanol synthesis purge gas coupling high-purity hydrogen device, which comprises a coal-to-methanol production line and also comprises a high-purity hydrogen device, wherein the high-purity hydrogen device comprises an air inlet buffer tank, a pressure swing adsorption device, a product gas buffer tank, a hydrogen filling compressor, an analysis gas buffer tank, an analysis gas compressor and a conveying pipeline, the air inlet buffer tank is communicated with a methanol synthesis device and is communicated with the pressure swing adsorption device, the product gas of the pressure swing adsorption device is conveyed to the product gas buffer tank, the product gas buffer tank is communicated with a synthesis gas pipe network and the hydrogen filling compressor, an analysis gas outlet of the pressure swing adsorption device is communicated with an air inlet of the analysis gas buffer tank, and an air outlet of the analysis gas buffer tank is communicated with a fuel gas pipe network through the analysis gas compressor. The utility model can not only utilize the methanol purge gas to produce high-purity hydrogen, but also promote the development of peripheral new energy industries.
Description
Technical Field
The utility model relates to the technical field of hydrogen recovery, in particular to a coal-to-methanol synthesis purge gas coupling high-purity hydrogen device.
Background
In the operation process of the methanol synthesis system, because a plurality of side reactions exist in the methanol synthesis, a large amount of inert gas is generated and continuously accumulated in the system, the normal operation of the methanol synthesis working condition is influenced, and in order to maintain the normal and stable operation of the device, the gas influencing the operation of the system must be continuously discharged, and the discharged gas is called purge gas, and the purge gas can cause a certain hydrogen loss. In order to reduce the hydrogen loss, a hydrogen recovery facility (membrane recovery) is generally added on the existing device, the recovered hydrogen is returned to the system for reuse, and unretracted gas is sent to the pulverized coal gasification device hot blast stove to be used as fuel, so that the utilization rate of purge gas is low, and the added value is low.
Disclosure of Invention
In order to solve the technical problems, the utility model provides a coal-to-methanol synthesis purge gas coupling high-purity hydrogen device, which aims to improve the recycling value of the purge gas.
In order to achieve the above object, the technical scheme of the present utility model is as follows:
the device comprises a coal-to-methanol production line, wherein the coal-to-methanol production line comprises a gasification device, a conversion device, a low-temperature methanol washing device, a synthesis gas compression device, a methanol synthesis device, a methanol rectification device and a hydrogen recovery device, a synthesis gas pipe network is arranged between the hydrogen recovery device and the synthesis gas compression device, and a fuel gas pipe network is arranged between the hydrogen recovery device and the gasification device and further comprises a high-purity hydrogen device;
the high-purity hydrogen device comprises an air inlet buffer tank, a pressure swing adsorption device, a product gas buffer tank, a hydrogen filling compressor, a desorption gas buffer tank, a desorption gas compressor and a conveying pipeline;
the gas inlet of the gas inlet buffer tank is communicated with the methanol synthesis device, the gas outlet of the gas inlet buffer tank is communicated with the gas inlet of the pressure swing adsorption device, the product gas outlet of the pressure swing adsorption device is communicated with the gas inlet of the product gas buffer tank, the gas outlet of the product gas buffer tank is communicated with the synthesis gas pipe network and the hydrogen filling compressor, the analysis gas outlet of the pressure swing adsorption device is communicated with the gas inlet of the analysis gas buffer tank, and the gas outlet of the analysis gas buffer tank is communicated with the fuel gas pipe network through the analysis gas compressor.
Further, a first regulating valve is arranged between the air inlet buffer tank and the methanol synthesis device, a second regulating valve is arranged between the hydrogen recovery device and the methanol synthesis device, the first regulating valve and the second regulating valve form a linkage effect, and when the first regulating valve is opened for a large flow, the second regulating valve is closed for a small flow.
Further, a third regulating valve is arranged between the air inlet buffer tank and the pressure swing adsorption device.
Further, a fourth regulating valve is arranged between the product gas buffer tank and the hydrogen filling compressor, a fifth regulating valve is arranged between the product gas buffer tank and the synthetic gas pipe network, a linkage effect is formed between the fourth regulating valve and the fifth regulating valve, and when the fourth regulating valve is opened, the fifth regulating valve is closed.
Further, a torch system is arranged on the coal-to-methanol production line and is connected with the fuel gas pipe network in parallel, and the torch system is respectively communicated with the analysis gas compressor and the hydrogen recovery device.
Further, a sixth regulating valve and a seventh regulating valve are respectively arranged between the analytic gas compressor and the torch system and between the analytic gas compressor and the fuel gas pipe network, the sixth regulating valve and the seventh regulating valve form a linkage effect, and when the sixth regulating valve is opened, the seventh regulating valve is closed.
Further, the inlet pressure of the first regulating valve is 5.0 MPaG-6.5 MPaG, the outlet pressure of the first regulating valve is 3.2MPaG, the compression pressure of the hydrogen filling compressor is 22MPaG, and the compression pressure of the analysis gas compressor is 0.5MPaG.
Further, when the hydrogen filling compressor is not started, the first regulating valve is closed for a small flow, the second regulating valve is opened for a large flow, the load of the pressure swing adsorption device is 30%, when the hydrogen filling compressor is started, the first regulating valve is opened for a large flow, the second regulating valve is closed for a small flow, and the load of the pressure swing adsorption device is 30% -120%.
Further, when the hydrogen filling compressor is started, the load of the pressure swing adsorption device is 80% -105%.
Through the technical scheme, the utility model has the beneficial effects that:
the utility model couples the high-purity hydrogen device with the hydrogen recovery device of the coal-to-methanol production line to produce high-purity hydrogen, thereby not only recovering the hydrogen in the methanol purge gas, but also creating economic benefits for sale.
The utility model can reduce the cost and price of the peripheral hydrogen energy, provide guarantee for hydrogen stations and industrial hydrogen in the peripheral area and promote the development of the peripheral new energy.
After the high-purity hydrogen device is coupled with the hydrogen recovery device of the coal-to-methanol production line, the utility model has no influence on the original coal-to-methanol production line, but can ensure intermittent supply of pure hydrogen, and the service life of the high-purity gas device is not damaged.
When high-purity hydrogen is not needed for filling, the utility model runs under low load, reduces the times of starting and stopping, and avoids unreasonable energy consumption and safety and environmental protection risks.
Drawings
FIG. 1 is a production flow diagram of the present utility model;
fig. 2 is a structural diagram of the high purity hydrogen generator and the hydrogen recovery device according to the present utility model.
The reference numerals in the drawings are: 1. a first regulating valve; 2. an intake buffer tank; 3. a third regulating valve; 4. a pressure swing adsorption apparatus; 5. a product gas buffer tank; 6. a fourth regulating valve; 7. a hydrogen filling compressor; 8. a fifth regulating valve; 9. analyzing the gas buffer tank; 10. a desorption gas compressor; 11. a seventh regulating valve; 12. a sixth regulating valve; 13. and a second regulating valve.
Detailed Description
The utility model is further described with reference to the drawings and detailed description which follow:
it should be noted that, in the following description, terms such as "front", "rear", "left", "right", "up", "down", "bottom" and "top" refer to directions in the drawings, and terms such as "inner" and "outer" refer to directions toward or away from a geometric center of a specific component, respectively.
1-2, a coal-to-methanol synthesis purge gas coupling high-purity hydrogen device comprises a coal-to-methanol production line, wherein the coal-to-methanol production line comprises a gasification device, a conversion device, a low-temperature methanol washing device, a synthesis gas compression device, a methanol synthesis device, a methanol rectification device and a hydrogen recovery device, a synthesis gas pipe network is arranged between the hydrogen recovery device and the synthesis gas compression device, a fuel gas pipe network is arranged between the hydrogen recovery device and the gasification device, the hydrogen recovery device adopts a membrane recovery process, permeation gas of the hydrogen recovery device is conveyed to the synthesis gas pipe network through a pipeline and then enters the synthesis gas compression device for recycling, and non-permeation gas of the hydrogen recovery device is conveyed to the fuel gas pipe network for boiler combustion and also comprises the high-purity hydrogen device;
the specific structure of the broken line part in fig. 1 is shown in fig. 2, and the high purity hydrogen device comprises an air inlet buffer tank 2, a pressure swing adsorption device 4, a product gas buffer tank 5, a hydrogen filling compressor 7, a desorption gas buffer tank 9, a desorption gas compressor 10 and a conveying pipeline;
the gas inlet of the gas inlet buffer tank 2 is communicated with the methanol synthesis device, the gas outlet of the gas inlet buffer tank 2 is communicated with the gas inlet of the pressure swing adsorption device 4, the finished gas outlet of the pressure swing adsorption device 4 is communicated with the gas inlet of the product gas buffer tank 5, the gas outlet of the product gas buffer tank 5 is communicated with the synthesis gas pipe network and the hydrogen filling compressor 7, the analysis gas outlet of the pressure swing adsorption device 4 is communicated with the gas inlet of the analysis gas buffer tank 9, and the gas outlet of the analysis gas buffer tank 9 is communicated with the fuel gas pipe network through the analysis gas compressor 10.
The utility model discloses a hydrogen recovery device, including the buffer tank that advances, be equipped with first governing valve 1 between buffer tank that advances 2 and the methanol synthesis device, first governing valve 1 is the relief pressure governing valve, is equipped with second governing valve 13 between hydrogen recovery device and the methanol synthesis device, first governing valve 1 forms the linkage effect with second governing valve 13, and when first governing valve 1 opened large-traffic, second governing valve 13 closes down the flow, distributes high purity hydrogen device and hydrogen recovery device's load, makes the total flow of first governing valve 1 and second governing valve 13 keep stable, first governing valve 1 cooperatees with second governing valve 13 and makes hydrogen recovery device's high purity hydrogen device handle the recovery and the utilization of hydrogen in the methanol purge gas jointly.
The hydrogen recovery device and the high-purity hydrogen device cooperatively treat the methanol purge gas, and when the high-purity hydrogen load is adjusted, the hydrogen recovery air inflow is synchronously changed, so that the methanol purge gas treatment capacity and the stability of components are maintained, the failure rate of the device can be effectively reduced, and the effective recovery and utilization of hydrogen in the methanol purge gas are realized.
The third regulating valve 3 is arranged between the air inlet buffer tank 2 and the pressure swing adsorption device 4, and the third regulating valve 3 is used for being matched with the air inlet buffer tank 2 to buffer and uniformly press, regulating the air inflow which is conveyed into the pressure swing adsorption device 4, and ensuring the normal operation of pressure swing adsorption.
A fourth regulating valve 6 is arranged between the product gas buffer tank 5 and the hydrogen filling compressor 7, a fifth regulating valve 8 is arranged between the product gas buffer tank 5 and the synthesis gas pipe network, a linkage effect is formed between the fourth regulating valve 6 and the fifth regulating valve 8, when the fourth regulating valve 6 is opened, the fifth regulating valve 8 is closed, and the fourth regulating valve 6 and the fifth regulating valve 8 jointly select the flow direction of hydrogen generated by the high-purity hydrogen device.
The flare system is connected in parallel with the fuel gas pipe network, and is respectively communicated with the analytic gas compressor 10 and the hydrogen recovery device, and during the driving process, the adjustment of the fuel gas pipe network or in a fault state, the non-permeation gas of the analytic gas and the hydrogen recovery device is discharged to the flare system through the sixth regulating valve 12 for combustion treatment.
The sixth regulating valve 12 and the seventh regulating valve 11 are respectively arranged between the analytic gas compressor 10 and the torch system and between the analytic gas compressor 10 and the fuel gas pipe network, the sixth regulating valve 12 and the seventh regulating valve 11 form a linkage effect, and when the sixth regulating valve 12 is opened, the seventh regulating valve 11 is closed.
The inlet pressure of the first regulating valve 1 is 5.0 MPaG-6.5 MPaG, the outlet pressure is 3.2MPaG, the compression pressure of the hydrogen filling compressor 7 is 22MPaG, and the compression pressure of the analysis gas compressor 10 is 0.5MPaG.
When the hydrogen filling compressor 7 is not started, the first regulating valve 1 is closed for low flow, the second regulating valve 13 is opened for high flow, the load of the pressure swing adsorption device 4 is 30%, when the hydrogen filling compressor 7 is started, the first regulating valve 1 is opened for high flow, the second regulating valve 13 is closed for low flow, and the load of the pressure swing adsorption device 4 is 30% -120%.
When the hydrogen filling compressor 7 is started, the load of the pressure swing adsorption device 4 is 80% -105%.
When the pressure-variable adsorption device is used, methanol purge gas of 5.0 MPaG-6.5 MPaG is firstly depressurized to 3.2MPaG through a conveying pipeline through a first regulating valve 1 and then enters an air inlet buffer tank 2, the air inlet buffer tank 2 is subjected to gas-liquid separation and buffering pressure equalizing, then the third regulating valve 3 is used for controlling the gas quantity entering the pressure-variable adsorption device 4, the hydrogen product gas treated by the pressure-variable adsorption device 4 enters a product gas buffer tank 5, and after the flow of the qualified product gas is regulated by a fourth regulating valve 6, the qualified product gas is pressurized to 22MPaG by a hydrogen filling compressor 7 for product filling.
The off-grade gas during start-up and stop or the hydrogen produced during system load adjustment are sent into a synthesis gas pipe network through a fifth regulating valve 8 to participate in the synthesis of the coal-to-methanol; the resolved gas of the pressure swing adsorption device 4 is collected and stabilized by a resolved gas buffer tank 9, then sent to a resolved gas compressor 10 for pressure rising to 0.5MPaG, and then sent to a fuel gas pipe network by a seventh regulating valve 11.
The high-purity hydrogen device can recycle gas to the methanol system in the start-stop debugging process, so that the environmental pollution caused by gas emptying in the debugging process is avoided, meanwhile, the running cost is reduced, the purge gas can effectively recycle hydrogen through high-purity hydrogen, the reduction of the hydrogen can reduce water brought into the pulverized coal system for combustion to a certain extent, the gas quality used by a hot blast stove in the pulverized coal gasification pressurizing device is optimized, and the use amount of fuel gas is reduced.
Because the current hydrogen transportation vehicles can only transport 350 kg-400 kg of hydrogen under high pressure of 22MPaG, the transportation quantity is small, the transportation cost is too high in proportion to the total cost of hydrogen, and generally the transportation cost of hydrogen can be one third of the total cost of hydrogen, and the transportation distance is limited, the utility model uses a high purity hydrogen device to couple with a methanol synthesis device to prepare high purity hydrogen with the purity of 99.999%, and accords with the hydrogen part 2 of GB/T3634.2-2011: the standard requirements of high-purity hydrogen in pure hydrogen, high-purity hydrogen and ultra-pure hydrogen are hydrogen products which can be used for vehicle transportation, and meanwhile, the product meets the requirements of GB/T37244-2018 fuel hydrogen for proton exchange membrane fuel cell vehicles, and industrial hydrogen and hydrogen fuel cell vehicles are hydrogenated for use, so that local hydrogen energy does not need long-distance transportation, the hydrogen cost is reduced, the development of new energy industry can be greatly promoted, the guarantee is provided for hydrogen stations in peripheral areas and industrial hydrogen, and the product is complementary with the current hydrogen energy development.
The method has the advantages that the method is not suitable for being used for selling, the purity of hydrogen produced by a high-purity hydrogen device is high, the hydrogen energy requirement is low in the market at present, the method is not suitable for specially building a production line to produce hydrogen for supporting the use of peripheral hydrogen, even if the hydrogen production line is built, the problem of frequent shutdown and reproduction caused by small peripheral hydrogen requirement is solved, the adverse effect on the service life of equipment is caused, the hydrogen cost is greatly improved, the problem is solved after the high-purity hydrogen device is coupled with the methanol synthesis device, when the hydrogen requirement is small, the high-purity hydrogen moves under a low load, the produced hydrogen returns to the methanol synthesis device for cyclic utilization, when the hydrogen is required, the load of the high-purity hydrogen device is opened, the hydrogen is produced, and the hydrogen extracted by the high-purity hydrogen can be obtained by utilizing the conversion device to carry out parameter adjustment, so that the problem of frequent shutdown and debugging of the high-purity hydrogen device is avoided, on the other hand, the problem of the production of the hydrogen is solved at any time, and the high-purity hydrogen device is avoided.
The preferred embodiments of the present utility model have been described in detail above with reference to the accompanying drawings, but the present utility model is not limited to the above examples, and various modifications can be made to the technical solution of the present utility model without departing from the spirit of the present utility model, i.e., the scope of the disclosure.
Claims (9)
1. The utility model provides a coal-to-methanol synthesis purge gas coupling high-purity hydrogen device, includes coal-to-methanol production line, coal-to-methanol production line includes gasification equipment, conversion equipment, low temperature methanol washing device, synthetic gas compression device, methanol synthesis device, methanol rectification device and hydrogen recovery device, there is the synthetic gas pipe network between hydrogen recovery device and the synthetic gas compression device, there is the fuel gas pipe network between hydrogen recovery device and the gasification device, its characterized in that still includes high-purity hydrogen device;
the high-purity hydrogen device comprises an air inlet buffer tank (2), a pressure swing adsorption device (4), a product gas buffer tank (5), a hydrogen filling compressor (7), a desorption gas buffer tank (9), a desorption gas compressor (10) and a conveying pipeline;
the gas inlet of the gas inlet buffer tank (2) is communicated with the methanol synthesis device, the gas outlet of the gas inlet buffer tank (2) is communicated with the gas inlet of the pressure swing adsorption device (4), the finished gas outlet of the pressure swing adsorption device (4) is communicated with the gas inlet of the product gas buffer tank (5), the gas outlet of the product gas buffer tank (5) is communicated with the synthesis gas pipe network and the hydrogen filling compressor (7), the analysis gas outlet of the pressure swing adsorption device (4) is communicated with the gas inlet of the analysis gas buffer tank (9), and the gas outlet of the analysis gas buffer tank (9) is communicated with the fuel gas pipe network through the analysis gas compressor (10).
2. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 1, wherein a first regulating valve (1) is arranged between the gas inlet buffer tank (2) and the methanol synthesis device, a second regulating valve (13) is arranged between the hydrogen recovery device and the methanol synthesis device, the first regulating valve (1) and the second regulating valve (13) form a linkage effect, and when the first regulating valve (1) is opened for a large flow, the second regulating valve (13) closes the flow.
3. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 1, wherein a third regulating valve (3) is arranged between the gas inlet buffer tank (2) and the pressure swing adsorption device (4).
4. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 1, wherein a fourth regulating valve (6) is arranged between the product gas buffer tank (5) and the hydrogen filling compressor (7), a fifth regulating valve (8) is arranged between the product gas buffer tank (5) and the synthesis gas pipe network, a linkage effect is formed between the fourth regulating valve (6) and the fifth regulating valve (8), and when the fourth regulating valve (6) is opened, the fifth regulating valve (8) is closed.
5. The coal-to-methanol synthesis purge gas coupling high-purity hydrogen device according to claim 1, wherein a torch system is arranged on the coal-to-methanol production line and is connected with a fuel gas pipe network in parallel, and the torch system is respectively communicated with a desorption gas compressor (10) and a hydrogen recovery device.
6. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 5, wherein a sixth regulating valve (12) and a seventh regulating valve (11) are respectively arranged between the analytic gas compressor (10) and the torch system and between the analytic gas compressor (10) and the fuel gas pipe network, the sixth regulating valve (12) and the seventh regulating valve (11) form a linkage effect, and when the sixth regulating valve (12) is opened, the seventh regulating valve (11) is closed.
7. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 2, wherein the inlet pressure of the first regulating valve (1) is 5.0 MPaG-6.5 MPaG, the outlet pressure is 3.2MPaG, the compression pressure of the hydrogen filling compressor (7) is 22MPaG, and the compression pressure of the desorption gas compressor (10) is 0.5MPaG.
8. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 2, wherein when the hydrogen filling compressor (7) is not started, the first regulating valve (1) is closed for low flow, the second regulating valve (13) is opened for high flow, the load of the pressure swing adsorption device (4) is 30%, when the hydrogen filling compressor (7) is started, the first regulating valve (1) is opened for high flow, the second regulating valve (13) is closed for low flow, and the load of the pressure swing adsorption device (4) is 30% -120%.
9. The coal-based methanol synthesis purge gas coupling high-purity hydrogen device according to claim 8, wherein the load of the pressure swing adsorption device (4) is 80% -105% when the hydrogen filling compressor (7) is started.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321961774.1U CN220425317U (en) | 2023-07-20 | 2023-07-20 | Coal-to-methanol synthesis purge gas coupling high-purity hydrogen device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321961774.1U CN220425317U (en) | 2023-07-20 | 2023-07-20 | Coal-to-methanol synthesis purge gas coupling high-purity hydrogen device |
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| CN220425317U true CN220425317U (en) | 2024-02-02 |
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| CN202321961774.1U Active CN220425317U (en) | 2023-07-20 | 2023-07-20 | Coal-to-methanol synthesis purge gas coupling high-purity hydrogen device |
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| CN (1) | CN220425317U (en) |
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2023
- 2023-07-20 CN CN202321961774.1U patent/CN220425317U/en active Active
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