CN211496938U - Membrane separation concentration hydrogen recovery device - Google Patents
Membrane separation concentration hydrogen recovery device Download PDFInfo
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- CN211496938U CN211496938U CN201921815651.0U CN201921815651U CN211496938U CN 211496938 U CN211496938 U CN 211496938U CN 201921815651 U CN201921815651 U CN 201921815651U CN 211496938 U CN211496938 U CN 211496938U
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Abstract
The utility model belongs to the chemical industry field relates to the hydrogen extraction technique among the chemical industry field, specifically is a concentrated hydrogen recovery device of membrane separation, including being equipped with the cold machine of doing, the filter, membrane separating mechanism, the cold machine of doing links to each other with the filter, and the filter links to each other with membrane separating mechanism, and membrane separating mechanism is equipped with the membrane separator, the vacuum pump, backflow pipeline and pressure regulating valve, and the membrane separator links to each other with the vacuum pump, and pressure regulating valve one end is established on the connection between membrane separator and vacuum pump, and one end links to each other with the vacuum pump, and the hydrogen product is through the vacuum pump output, and the fuel gas. The vacuum system is adopted to reduce the pressure of the hydrogen permeation side of the membrane separation device, the partial pressure difference of hydrogen on the two sides of the membrane is improved, the permeation driving force of the hydrogen on the surface of the membrane is improved, the permeation efficiency of the hydrogen on the surface of the membrane can be improved by 15-40%, and the energy consumption and the operation cost of the membrane separation device can be obviously reduced.
Description
Technical Field
The utility model belongs to the technical field of hydrogen draws, especially, relate to a concentrated hydrogen recovery device of membrane separation.
Background
Hydrogen is an important resource in novel energy and petrochemical industry, and the prior technology for separating and recovering hydrogen from hydrogen-containing mixed gas mainly comprises a pressure swing adsorption method and a membrane separation method.
The pressure swing adsorption method is to utilize the characteristic that the adsorption capacity, adsorption force and adsorption speed of the adsorbent to different gases are different with the difference of pressure, to pressurize and adsorb easily-adsorbed components in the mixture under the condition of selective adsorption of the adsorbent, and to desorb the adsorbed components when the pressure of the adsorbent bed is reduced, thereby regenerating the adsorbent. The pressure swing adsorption method has the advantages of high regeneration speed, low energy consumption, simple operation and mature and stable process. The method has the greatest advantages that the hydrogen with high product purity (99.99%) can be obtained, and the hydrogen recovery rate is about 85-90%. However, the number of adsorbers is large, and the occupied area is large.
The membrane separation method is realized by means of the difference of the permeability of each component of gas in the membrane, and the osmotic driving force is the partial pressure difference of two sides of the membrane. The membrane separation technology has the advantages of simple process, large operation flexibility, low cost and the like. However, the purity of hydrogen recovered by membrane separation is not high, and a relatively high pressure is required for the feed gas.
For the hydrogen-containing gas with the pressure of dry gas of an oil refinery being 0.2Mpa to 1.0Mpa and the hydrogen content being 20 percent to 60 percent, the technical problems of low membrane separation efficiency, large dosage of membrane material and high investment cost exist because the permeation driving force of the hydrogen on the membrane surface is small. Therefore, the low-content hydrogen recovery needs to be pressurized, the membrane separation needs to be carried out by adopting a mode of compressing and pressurizing the hydrogen-containing feed gas under 1.5-3.0 Mpa, the hydrogen with high recovery rate can be obtained, and the technical problems of high cost of a compressor and high pressurization energy consumption also exist.
If the raw material hydrogen is not pressurized, the hydrogen product amount is small, and the hydrogen recovery rate is low, so that the method has no economic value.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides a hydrogen device is retrieved in membrane separation concentration has overcome the restriction that conventional membrane separation method need compress the pressurization to operate under higher pressure under the lower condition of raw materials hydrogen content to the raw materials of lower concentration hydrogen, adopts the method of managing to find time to the membrane infiltration side can not pressurize the raw materials, and the energy consumption is low, the small investment, and is with low costs.
Solve above technical problem the utility model provides a concentrated hydrogen recovery device of membrane separation, its characterized in that: the device comprises a freeze drying machine, a filter and a membrane separation mechanism, wherein the freeze drying machine is connected with the filter, the filter is connected with the membrane separation mechanism, the membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, the membrane separator is connected with the vacuum pump, one end of the pressure regulating valve is arranged on the connection between the membrane separator and the vacuum pump, one end of the pressure regulating valve is connected with the vacuum pump, a hydrogen product is output through the vacuum pump, and fuel gas is output through the membrane separator.
The membrane separator membrane is provided with a retentate side and a permeate side, the permeate side is connected with the vacuum pump, and the retentate side is connected with the filter and the fuel gas device.
The device also comprises a pressure swing adsorber which is connected with a vacuum pump. After the pressure of the hydrogen product obtained after evacuation is increased, the hydrogen product is further purified by a pressure swing adsorber to obtain pure hydrogen or a high-purity hydrogen product.
The device is also provided with a heater, one end of the heater is connected with the cold dryer, and the other end of the heater is connected with the filter.
The temperature of the heater is 20-80 ℃.
The pressure of the membrane separator at the permeation side is-0.04 to-0.09 Mpa.
The pressure of the membrane separator at the permeation side is-0.081 to-0.085 Mpa.
The temperature of the cold dryer is 2-10 ℃, and the pressure value is 0.2-1.0 Mpa.
The pressure of the surplus side of the membrane separation hydrogen recovery device is 0.2-1.0 Mpa.
The utility model discloses a method for concentrated recovery of hydrogen of well membrane separation, the step is as follows:
(1) hydrogen-containing gas enters a cold dryer to remove liquid hydrocarbon components and liquid water;
(2) removing trace solid particle impurities in the gas through a filter;
(3) hydrogen is purified in a membrane separator, and the pressure of the permeation side is reduced and stably maintained by a vacuum pump, a backflow pipeline and a pressure regulating valve which are connected with the permeation side of the membrane separator;
(4) hydrogen on the membrane permeation side is obtained after evacuation and is output as a hydrogen product;
(5) the gas on the membrane retentate side is discharged from the membrane separator and enters a factory fuel gas pipe network to be used as fuel.
Hydrogen is obtained from the outlet of the evacuation system, and the residual gas after hydrogen separation is discharged out of the membrane separator as fuel gas.
Hydrogen-containing gas enters a cold dryer to remove liquid substances such as hydrocarbon components, water and the like, then a filter is used for removing trace solid particle impurities in the gas, finally the gas enters a vacuum membrane separation device for purifying hydrogen, and a vacuum pump, a backflow pipeline and a pressure regulating valve which are connected with the permeation side of the membrane reduce and stabilize the permeation side pressure to a lower pressure; hydrogen on the permeation side is obtained through a pumping system and is output as a hydrogen product; the gas on the residual side enters a factory fuel gas pipe network to be used as fuel. Hydrogen is obtained from the outlet of the evacuation system, and the residual gas after hydrogen separation is discharged from the membrane separation device as fuel gas.
The hydrogen purification is carried out by adopting a vacuum membrane separation mechanism, the vacuum membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, two ends of the pressure regulating valve are respectively connected with the membrane separator and the vacuum pump, the vacuum pump is connected with the membrane separator, and the membrane separator, the vacuum pump and the pressure regulating valve are mutually connected through the backflow pipeline. When the vacuum pump and the pressure regulating valve are adopted to pump the permeation side of the membrane separator, the hydrogen at the outlet of a part of vacuum pump flows back to the permeation side of the membrane separator to ensure the stability of the permeation side pressure.
The hydrogen-containing gas is refinery hydrogen-containing fuel gas with 20-60% hydrogen content or other hydrogen-containing gas, and the pressure value is 0.2-1.0 MPa.
The pressure control valve with reflux can stabilize the vacuum pressure at the permeation side, and the pressure at the permeation side is matched with the fuel pipe network to be used as fuel.
The utility model discloses utilize the difference of the gas pressure difference of both sides and fuel gas and hydrogen permeation rate among the mist, the selective hydrogen that sees through to reach the effect of separation. Hydrogen was delivered by a vacuum pump. The hydrogen is selectively separated from the fuel gas, resulting in improved hydrogen recovery.
The utility model has the medium pressure of 0.2 Mpa-1.0 Mpa, other hydrogen-containing gases such as hydrogen-containing fuel gas of oil refineries with the hydrogen content of 20% -60%, enters a cold dryer to remove liquid substances such as hydrocarbon components, water and the like, and then is filtered to remove trace solid particle impurities in the gas, purifying hydrogen in a vacuum membrane separation device consisting of a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, reducing and stabilizing the pressure of the permeation side to a lower pressure by the vacuum pump, the backflow pipeline and the pressure regulating valve which are connected with the permeation side of the membrane, because the vacuum system reduces the pressure at the permeation side, the partial pressure difference at two sides of the membrane as the driving force of hydrogen permeation is obviously improved, the permeation efficiency of hydrogen in the membrane device is improved, compared with the prior membrane separation hydrogen recovery device which does not perform evacuation and depressurization on the permeation side, the membrane consumption can be reduced, the cost is reduced, the hydrogen yield is increased, and the economic benefit is improved.
The utility model discloses in adopt vacuum system to reduce the pressure of membrane separation device hydrogen permeation side, can not pressurize the feed gas, improved the partial pressure difference of hydrogen in membrane both sides hydrogen, improved the infiltration driving force of hydrogen on the membrane surface, with the current membrane separation device comparison of not managing to find time the decompression to membrane separation unit hydrogen permeation side, hydrogen can improve 15% ~ 40% at the osmotic efficiency on membrane surface. Compared with the conventional method of pressurizing the raw material gas of the membrane separation device and increasing the partial pressure difference of hydrogen on two sides of the membrane, the method can obviously reduce the energy consumption and the operation cost of the membrane separation device.
The utility model discloses the method that the infiltration side was managed to find time is mainly applicable to the raw materials gas of pressure 0.2Mpa ~ 1.0Mpa hydrogen content 20% ~ 60%, is particularly useful for the raw materials gas of hydrogen content at 20% ~ 30%.
Drawings
FIG. 1 and FIG. 2 are schematic diagrams of the structure of the middle device of the present invention
FIG. 3 is a flow chart of the process of the present invention
Wherein, the marks in the figure are specifically: 1. cold drying machine, 2 filter, 3 membrane separator (3-1 permeation side, 3-2 permeation side), 4 vacuum pump, 5 pressure regulating valve, 6 heater, 7 fuel gas device and 8 pressure swing adsorption device
Detailed Description
The present invention will be described in further detail with reference to the following embodiments, wherein the used equipments and instruments are conventional equipments and instruments, and the freeze drying machine, the filter, the membrane separator, the vacuum pump and the pressure regulating valve are conventional general equipments in the technical field, and can be purchased from the market:
example 1
The system device for recovering hydrogen after membrane separation and concentration is provided with a freeze drying machine, a filter and a vacuum membrane separation mechanism, wherein the freeze drying machine is connected with the filter, the filter is connected with the vacuum membrane separation mechanism, the vacuum membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, the membrane separator is connected with the vacuum pump, one end of the pressure regulating valve is arranged on the connection between the membrane separator and the vacuum pump, the other end of the pressure regulating valve is connected with the vacuum pump, a hydrogen product is output through the vacuum pump, and fuel gas is output through the membrane separator. The membrane separator membrane is provided with a retentate side and a permeate side, the permeate side is connected with a vacuum pump, and the retentate side is connected with a filter and a fuel gas device. The device also comprises a pressure swing adsorber which is connected with a vacuum pump.
The pressure of the membrane separator at the permeation side is-0.04 or-0.09 MPa. The temperature of the cold dryer is 2 ℃, the pressure value is 1.0Mpa, and the pressure of the retentate side of the membrane separation hydrogen recovery device is 0.95 Mpa.
Introducing hydrogen-containing fuel gas of oil refinery with pressure of 1.0Mpa into vacuum membrane separator, evacuating the permeation side of membrane separator by evacuation, maintaining the pressure of permeation side at-0.04 or-0.09 Mpa, obtaining hydrogen gas from the outlet of evacuation system, and discharging the residual gas after hydrogen separation as fuel gas out of membrane separator.
The hydrogen gas with the available value obtained in the utility model is the hydrogen with the content of more than 80 percent, and generally, the hydrogen with the content of more than 95 percent can be directly used in the chemical process, and sometimes 80 percent can also be used.
Example 2
The system device for recovering hydrogen after membrane separation and concentration is provided with a freeze drying machine, a filter and a vacuum membrane separation mechanism, wherein the freeze drying machine is connected with the filter, the filter is connected with the vacuum membrane separation mechanism, the vacuum membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, the membrane separator is connected with the vacuum pump, one end of the pressure regulating valve is arranged on the connection between the membrane separator and the vacuum pump, the other end of the pressure regulating valve is connected with the vacuum pump, a hydrogen product is output through the vacuum pump, and fuel gas is output through the membrane separator.
The membrane separator membrane is provided with a retentate side and a permeate side, the permeate side is connected with a vacuum pump, and the retentate side is connected with a filter and a fuel gas device. The device also comprises a pressure swing adsorber which is connected with a vacuum pump. After the pressure of the hydrogen product obtained after evacuation is increased, the hydrogen product is further purified by a pressure swing adsorber to obtain pure hydrogen or a high-purity hydrogen product.
The pressure of the permeation side of the membrane separator is-0.081 Mpa or-0.085 Mpa, the temperature of the freeze-drying machine is 10 ℃, the pressure value is 0.2Mpa, and the pressure of the permeation side of the hydrogen recovery device by membrane separation is 0.15 Mpa.
Example 3
The system device for recovering hydrogen after membrane separation concentration is provided with a freeze drying machine, an electric heater, a filter and a vacuum membrane separation mechanism, wherein the freeze drying machine is connected with the heater, the heater is connected with the filter, the filter is connected with the vacuum membrane separation mechanism, the vacuum membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, the membrane separator is connected with the vacuum pump, one end of the pressure regulating valve is arranged on the connection between the membrane separator and the vacuum pump, the other end of the pressure regulating valve is connected with the vacuum pump, a hydrogen product is output through the vacuum pump, and fuel gas is output through.
The membrane separator membrane is provided with a retentate side and a permeate side, the permeate side is connected with a vacuum pump, and the retentate side is connected with a filter and a fuel gas device. The device also comprises a pressure swing adsorber which is connected with a vacuum pump. After the pressure of the hydrogen product obtained after evacuation is increased, the hydrogen product is further purified by a pressure swing adsorber to obtain pure hydrogen or a high-purity hydrogen product. The heater temperature is 20 deg.C, 60 deg.C or 80 deg.C, and the pressure of the membrane separator permeation side is-0.06 Mpa or-0.083 Mpa. The temperature of the cold dryer is 2-10 ℃, the pressure value is 0.2-1.0 Mpa, and the pressure of the retentate side of the membrane separation hydrogen recovery device is 0.2-1.0 Mpa.
Example 4
The raw material gas composition is as follows: TABLE 1
Other contents are as in example 3, the refinery reforming pressure swing adsorption hydrogen extraction gas with the composition content as above is fed into a freeze drying machine under the conditions of 0.5MPa and 40 ℃ to remove liquid substances such as hydrocarbon components, water and the like, fed into a filter to remove trace solid particle impurities therein, fed into a vacuum membrane separation device consisting of a membrane piece, a vacuum pump, a backflow pipeline and a pressure regulating valve to purify hydrogen, the pressure of the permeation side of the membrane is reduced and stabilized to-0.085 MPa by the vacuum pump, the permeation side of the membrane is pumped out by the vacuum pump (except for a part of the permeation side which returns to the membrane unit to stabilize the pressure), and a hydrogen-rich product is obtained and fed into a refinery hydrogenation device to be used as a hydrogenation raw material, and the residual gas which does not pass through the membrane is discharged into a plant fuel gas pipe network to be used as fuel.
In this example, the purity of hydrogen was 98% and the yield of hydrogen was 93%.
Example 5
The raw material gas composition is as follows: TABLE 2
| Composition of | H2 | N2 | CH4 | C2H4 | C2H6 | C3H8 | C4 | C5+ |
| V％ | 26.3 | 14.2 | 27.3 | 15.6 | 12.7 | 0.82 | 0.6 | 2.48 |
Other contents are as example 3, the refinery catalytic cracking dry gas with the composition content as above is sent into a cold dryer under the conditions of 0.7MPa and 40 ℃ to remove liquid substances such as hydrocarbon components, water and the like, and then sent into a filter to remove trace solid particle impurities therein, and then sent into a vacuum membrane separation device consisting of a membrane piece, a vacuum pump, a backflow pipeline and a pressure regulating valve to purify hydrogen, the vacuum pump, the backflow pipeline and the pressure regulating valve connected with the permeation side of the membrane reduce the pressure of the permeation side to-0.081 MPa, hydrogen-rich permeation gas is pumped out by the vacuum pump (except for a part of pressure returned to the membrane unit to stabilize pressure) to obtain a hydrogen-rich product which is sent to a hydrogenation device of a refinery to be used as a hydrogenation raw material, and residual gas which does not pass through the membrane is discharged into a fuel gas pipe.
In this example, the purity of hydrogen was 93% and the yield of hydrogen was 80%.
Example 6
The raw material gas composition is as follows: TABLE 3
| Composition of | H2 | C1 | C2 | C3 | C4 | C5 | C6 | C7+ |
| V％ | 29.6 | 42.9 | 15.2 | 6.5 | 3.6 | 1.2 | 0.8 | 0.2 |
Other contents are as example 3, refinery fuel gas with the composition content as above is fed into a freeze drying machine under the conditions of 0.3MPa and 30 ℃ to remove liquid substances such as hydrocarbon components, water and the like, fed into a filter to remove trace solid particle impurities therein, fed into a vacuum membrane separation device consisting of a membrane piece, a vacuum pump, a backflow pipeline and a pressure regulating valve to purify hydrogen, the pressure of the permeation side of the membrane is reduced and stabilized to-0.09 MPa by the vacuum pump, the permeation side of the hydrogen-rich permeation gas is pumped out by the vacuum pump (except for a small part of the permeation gas which returns to the membrane unit to stabilize the pressure) to obtain a hydrogen-rich product, the hydrogen-rich product is sent to a hydrogenation device of an oil refinery to be used as hydrogenation raw material, and the residual gas which does not pass through the membrane is discharged into a fuel.
In this example, the purity of hydrogen was 92% and the yield of hydrogen was 75%.
Test one:
the raw material gas composition is as follows: TABLE 4
| Composition of | H2 | C1 | C2 | C3 | C4+ |
| V％ | 27.1 | 45.6 | 17.1 | 4.2 | 6.0 |
Other operation steps are the same, equipment is the same, refinery fuel gas with the composition content as the above is fed into a freeze drying machine under the conditions of 0.2MPa and 30 ℃ to remove liquid substances such as hydrocarbon components, water and the like, the refinery fuel gas is fed into a filter to remove trace solid particle impurities, and then the refinery fuel gas is respectively fed into a separation device only provided with a membrane and a vacuum membrane separation device consisting of the membrane, a vacuum pump, a backflow pipeline and a pressure regulating valve to purify hydrogen (the performance and the model of the membrane of the two devices are the same), the permeation test of the membrane of the corresponding separation device only provided with the membrane is kept at normal pressure, and the permeation side of the membrane of the vacuum membrane separation device consisting of the membrane, the vacuum pump, the backflow pipeline and the pressure regulating valve is stably kept at the vacuum degree of-0.. The experimental results comparing the two different processes described above are as follows:
TABLE 5
| Test number | Whether or not to evacuate | Permeate side pressure | Purity of hydrogen | Hydrogen recovery rate |
| 1 | Whether or not | 0 | 70.97 | 11.71 |
| 2 | Is that | -0.081MPa | 90.15 | 56.97 |
Compared with the existing membrane separation device which does not perform evacuation depressurization on the hydrogen permeation side of the membrane separation unit, the permeation efficiency of hydrogen on the membrane surface can be improved by 15-40%. Under the conditions of lower pressure and hydrogen purity, more than 80% of hydrogen can not be obtained without vacuumizing the permeation side, and the hydrogen permeability is only about 10%, so that the method has no practical use value. After the hydrogen permeation side is evacuated, the content of the hydrogen product can be more than 85%, and the hydrogen transmission rate is 50-90% and has practical use value.
Test No. two
The raw material gas composition is as follows: TABLE 6
| Composition of | H2 | N2 | C1 | C2 | C3 | C4 | C5+ |
| V％ | 26.3 | 8.3 | 28.3 | 18.9 | 14.2 | 2.3 | 1.7 |
Other operation steps are the same, equipment is the same, refinery fuel gas with the composition content as shown in the table is fed into a freeze drying machine at the temperature of 30 ℃ below zero to remove liquid substances such as hydrocarbon components, water and the like, fed into a filter to remove trace solid particle impurities in the refinery fuel gas, and fed into a separation device only provided with a membrane piece at the pressure of 0.8MPa, and the permeation test of the membrane is kept at normal pressure; the hydrogen is purified by entering a vacuum membrane separation device consisting of a membrane piece, a vacuum pump, a reflux pipeline and a pressure regulating valve under the pressure of 0.2MPa (the performance and the model of the membrane piece of the two devices are the same), and the permeation side of the membrane is stably kept to the vacuum degree of-0.085 MPa. The experimental results comparing the two different processes described above are as follows:
TABLE 7
| Test number | Test pressure | Whether or not to evacuate | Permeate side pressure | Purity of hydrogen | Yield of hydrogen |
| 1 | 0.8MPa | Whether or not | 0 | 81.65 | 84.45 |
| 2 | 0.2MPa | Is that | -0.085MPa | 88.66 | 89.46 |
Compared with the conventional method of pressurizing the feed gas of the membrane separation device and increasing the partial pressure difference of hydrogen on two sides of the membrane, the feed gas with the same partial pressure difference needs to be increased by 4-5 times.
While the foregoing shows and describes the fundamental principles and principal features of the invention, together with the advantages thereof, the foregoing embodiments and description are illustrative only of the principles of the invention, and various changes and modifications can be made therein without departing from the spirit and scope of the invention, which will fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (9)
1. The utility model provides a membrane separation is concentrated and is retrieved hydrogen device which characterized in that: the device comprises a freeze drying machine, a filter and a membrane separation mechanism, wherein the freeze drying machine is connected with the filter, the filter is connected with the membrane separation mechanism, the membrane separation mechanism is provided with a membrane separator, a vacuum pump, a backflow pipeline and a pressure regulating valve, the membrane separator is connected with the vacuum pump, one end of the pressure regulating valve is arranged on the connection between the membrane separator and the vacuum pump, one end of the pressure regulating valve is connected with the vacuum pump, a hydrogen product is output through the vacuum pump, and fuel gas is output through the membrane separator.
2. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the membrane separator membrane is provided with a retentate side and a permeate side, the permeate side is connected with the vacuum pump, and the retentate side is connected with the filter and the fuel gas device.
3. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the device also comprises a pressure swing adsorber which is connected with a vacuum pump.
4. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the device is also provided with a heater, one end of the heater is connected with the cold dryer, and the other end of the heater is connected with the filter.
5. The membrane separation and concentration hydrogen recovery device according to claim 4, wherein: the temperature of the heater is 20-80 ℃.
6. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the pressure of the membrane separator at the permeation side is-0.04 to-0.09 Mpa.
7. The membrane separation and concentration hydrogen recovery device according to claim 6, wherein: the pressure of the membrane separator at the permeation side is-0.081 to-0.085 Mpa.
8. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the temperature of the cold dryer is 2-10 ℃, and the pressure value is 0.2-1.0 Mpa.
9. The membrane separation and concentration hydrogen recovery device according to claim 1, wherein: the pressure of the surplus side of the membrane separation hydrogen recovery device is 0.2-1.0 Mpa.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110697655A (en) * | 2019-10-25 | 2020-01-17 | 昊华化工科技集团股份有限公司 | Method and system device for recovering hydrogen through membrane separation and concentration |
| WO2023287905A1 (en) * | 2021-07-14 | 2023-01-19 | Ohmium International, Inc. | Systems and methods for hydrogen recovery |
| US11767599B2 (en) | 2019-11-21 | 2023-09-26 | Ohmium International, Inc. | Electrochemical devices, modules, and systems for hydrogen generation and methods of operating thereof |
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2019
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110697655A (en) * | 2019-10-25 | 2020-01-17 | 昊华化工科技集团股份有限公司 | Method and system device for recovering hydrogen through membrane separation and concentration |
| CN110697655B (en) * | 2019-10-25 | 2024-06-14 | 西南化工研究设计院有限公司 | Method and system device for recovering hydrogen through membrane separation concentration |
| US11767599B2 (en) | 2019-11-21 | 2023-09-26 | Ohmium International, Inc. | Electrochemical devices, modules, and systems for hydrogen generation and methods of operating thereof |
| WO2023287905A1 (en) * | 2021-07-14 | 2023-01-19 | Ohmium International, Inc. | Systems and methods for hydrogen recovery |
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