CN115364632A - Secondary recycling system and method for hydrogen production separation liquid - Google Patents
Secondary recycling system and method for hydrogen production separation liquid Download PDFInfo
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- CN115364632A CN115364632A CN202211012034.3A CN202211012034A CN115364632A CN 115364632 A CN115364632 A CN 115364632A CN 202211012034 A CN202211012034 A CN 202211012034A CN 115364632 A CN115364632 A CN 115364632A
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- 239000007788 liquid Substances 0.000 title claims abstract description 170
- 238000000926 separation method Methods 0.000 title claims abstract description 46
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 239000001257 hydrogen Substances 0.000 title claims abstract description 42
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 36
- 238000004064 recycling Methods 0.000 title claims abstract description 19
- 238000000034 method Methods 0.000 title claims abstract description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 180
- 239000003513 alkali Substances 0.000 claims abstract description 38
- 208000028659 discharge Diseases 0.000 claims abstract description 19
- 239000000203 mixture Substances 0.000 claims abstract description 12
- 238000001035 drying Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 50
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 23
- 238000012545 processing Methods 0.000 claims description 18
- 230000003020 moisturizing effect Effects 0.000 claims description 12
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 238000005868 electrolysis reaction Methods 0.000 claims description 10
- 238000000746 purification Methods 0.000 claims description 7
- 230000005484 gravity Effects 0.000 claims description 6
- 230000001502 supplementing effect Effects 0.000 claims description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 238000012544 monitoring process Methods 0.000 claims description 3
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 5
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000013461 design Methods 0.000 abstract description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/38—Removing components of undefined structure
- B01D53/42—Basic components
-
- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Abstract
The invention discloses a secondary recycling system and a secondary recycling method for hydrogen production separation liquid, and the secondary recycling system comprises a gas-liquid separation module 1, a PLC (programmable logic controller) control module 2, a drying and purifying drainer 3, a liquid discharge treatment module 4 and a water replenishing module 5, wherein a gas-alkali mixture generated by hydrogen production separation is introduced into a first inlet end of the gas-liquid separation module 1, a second inlet end of the gas-liquid separation module 1 is communicated with a first inlet end of the liquid discharge treatment module 4 through a pipeline, an outlet end of the drying and purifying drainer 3 is communicated with a second inlet end of the liquid discharge treatment module 4 through a pipeline, an outlet end of the liquid discharge treatment module 4 is communicated with an inlet end of the water replenishing module 5 through a pipeline, and an outlet end of the water replenishing module 5 is communicated with an inlet end of the gas-liquid separation module 1 through a pipeline. The invention has the advantages that the liquid generated after gas-water separation is safely recovered and secondarily utilized, thereby realizing the recovery and the recycling of the liquid and replacing the design that the original discharged liquid is directly discharged into a water seal.
Description
Technical Field
The invention relates to the technical field of hydrogen production recovery systems, in particular to a secondary recovery and utilization system and a secondary recovery and utilization method for hydrogen production separation liquid.
Background
The hydrogen used as the energy storage carrier has the advantages of light weight, high energy density and no emission to the environment when in use. The existing hydrogen production technologies mainly comprise two major types of hydrogen production by mineral fuel and hydrogen production by water electrolysis. The hydrogen production by water electrolysis obtains high-purity hydrogen by water electrolysis, the technology is mature, the purity of the purified hydrogen can reach 99.9999 percent, which is one order of magnitude higher than that of other hydrogen production modes, and the prepared hydrogen does not contain carbon element impurities. Nowadays, the sustainable development of new energy is vigorously advocated in China, and hydrogen production by water electrolysis is met with new development opportunities. However, the existing basic water electrolysis hydrogen production equipment has the following disadvantages: firstly, the steam-water mixture generated after the electrolysis carries a large amount of steam out of high-temperature gas generated after the separation of the steam-water mixture by the gas-liquid separator, and liquid is discharged into the water seal after cooling. Secondly, the cooled liquid contains partial alkali liquor, and the cooled liquid cannot be treated in time after being discharged into a water seal to cause pollution. Thirdly, if the liquid discharge time after cooling is unreasonable to be controlled, or the cooling water temperature changes, either the liquid is discharged from the vent hole, or partial hydrogen is discharged along with the liquid, certain waste is formed, and the alkali liquor is discharged to be supplemented at regular time. Fourthly, the quality of the pure water is detected only at the water production end, and the pure water is deteriorated due to the microbial fermentation in the water tank and cannot meet the electrolysis requirement.
Disclosure of Invention
The invention aims to provide a secondary recycling system and a secondary recycling method for hydrogen production separation liquid, which are used for safely recycling and reutilizing the liquid generated after gas-water separation, and the liquid is recycled and reused by adding a liquid collector and a nitrogen-sealed water tank, so that the design that the original discharged liquid is directly discharged into a water seal is replaced.
The technical purpose of the invention is realized by the following technical scheme:
the utility model provides a secondary recycle system of hydrogen production separation liquid, its characterized in that, includes gas-liquid separation module 1, PLC control module 2, dry purification drainer 3, flowing back processing module 4 and moisturizing module 5, the first entry end of gas-liquid separation module 1 lets in the gas-alkali mixture that the hydrogen production separation produced, the second entry end of gas-liquid separation module 1 passes through the pipeline intercommunication with the first entry end of flowing back processing module 4, the pipeline intercommunication is crossed with the second entry end of flowing back processing module 4 to the exit end of dry purification drainer 3, the exit end of flowing back processing module 4 passes through the pipeline intercommunication with the entry end of moisturizing module 5, the exit end of moisturizing module 5 passes through the pipeline intercommunication with the entry end of gas-liquid separation module 1.
Preferably, the gas-liquid separation module 1 includes a gas-alkali separator 101, a scrubber 102, a gas cooler 103 and a gas-water separator 104, a gas-alkali mixture generated by hydrogen production separation is introduced into a first water inlet of the gas-alkali separator 101, a second water inlet of the gas-alkali separator 101 is communicated with the water replenishing module 5 through a pipeline, an exhaust port of the gas-alkali separator 101 is communicated with an air inlet of the scrubber 102 through a pipeline, an exhaust port of the scrubber 102 is communicated with an air inlet of the gas cooler 103, an exhaust port of the gas cooler 103 is communicated with an air inlet of the gas-water separator 104 through a pipeline, a drain port of the gas cooler 103 is communicated with the liquid discharge processing module 4 through a pipeline, and a drain port of the gas-water separator 104 is communicated with the liquid discharge processing module 4 through a pipeline.
Preferably, the water replenishing module 5 comprises a water tank 501, a water replenishing pump 502 and a back pressure valve 503, the water inlet of the water tank 501 is communicated with the liquid discharge processing module 4 through a pipeline, the air outlet of the water tank 501 is communicated with the back pressure valve 503, the water inlet of the water replenishing pump 502 is communicated with the water outlet of the water tank 501, and the water tank 501 is further provided with a nitrogen inlet.
Preferably, the liquid discharge treatment module 4 comprises a liquid level meter 401 and a liquid collector 402, the liquid level meter 401 is arranged inside the liquid collector 402, a first water inlet of the liquid collector 402 is communicated with a water outlet of the gas cooler 103 and a water outlet of the gas-water separator 104 through pipelines, a second water inlet of the liquid collector 402 is communicated with a water outlet of the drying and purifying water discharger 3 through a pipeline, and a water outlet of the liquid collector 402 is communicated with a water inlet of the water tank 501 through a pipeline.
Preferably, a first on-off valve 201 is arranged at a first water inlet of the liquid trap 402, a second on-off valve 202 is arranged at a water outlet of the liquid trap 402, and a third on-off valve 203 is arranged at a nitrogen inlet of the water tank 501.
Preferably, a high liquid level point 402b and a low liquid level point 402a are arranged in two layers of the liquid level meter 401 in the liquid collector 402.
Preferably, the PLC control module 2 is connected to the first switch valve 201, the second switch valve 202, the third switch valve 203, the liquid level meter 401, and the water replenishing pump 502, and the PLC control module 2 controls the opening and closing of the first switch valve 201, the second switch valve 202, the third switch valve 203, and the water replenishing pump 502 by monitoring the liquid level in the liquid trap 402 through the liquid level meter 401.
A secondary recycling method of hydrogen production separation liquid is characterized by comprising the following specific steps:
gas-alkali mixture generated by electrolysis of the hydrogen production electrolytic cell enters a gas-alkali separator 101, the temperature in the gas is high at the moment, the content of water vapor and alkali is extremely high, the gas is filtered by a cleaner 102, the alkali content in the gas is reduced, the temperature of the gas is reduced by a cooler 103, water in the gas is condensed into liquid, the water vapor content in the gas is reduced, part of separated liquid water remains in the cooler 103, the separated gas and part of liquid water enter a gas-water separator 104, a first switch valve 201 is opened after a period of time by a PLC control module 2, and the liquid water in the cooler 103 and the gas-water separator 104 flows to a liquid collector 401 under the drive of system pressure and gravity;
the water collected by the drying and purifying drainage module 3 flows to the liquid collector 401 through a bottom pipeline, the liquid level meter 401 at the top end of the liquid collector 401 monitors the liquid level, a signal returns to the PLC control module 2, when a set high liquid level point 402b is reached, the PLC control module 2 controls to open the second switch valve 202, the liquid in the liquid collector 401 flows to the water replenishing tank 501 under the drive of the pressure and gravity, when the liquid level is lowered to a low liquid level point 402a, the PLC control module 2 controls to close the second switch valve 202, at the moment, after the liquid generated by the system operation is replenished into the water tank 501, the water replenishing pump 502 is controlled to be opened through the PLC control module 2 to replenish the gas-alkali separator 101;
in order to prevent the mixed gas dangerous source caused by the release of the gas dissolved in the liquid in the water tank 501 and ensure that no oxygen exists in the water replenishing tank 501 and no oxidation reaction occurs in water, the PLC control module 2 is controlled to periodically open the third switch valve 203 on the water tank 501 to flush nitrogen into the water tank 501 for replacement so as to form micro-pressure nitrogen protection, the pressure of a micro-pressure system is 50-200kPa, and the replacement gas is discharged through the back pressure valve 503.
In conclusion, the invention has the following beneficial effects:
according to the invention, the PLC control module is used for realizing safe recovery and secondary utilization of discharged liquid in the cooler, the gas-water separator and the drying and purifying drainer, and the original design that the discharged liquid is directly discharged into a water seal for discarding is replaced, so that the environmental pollution and waste are reduced, the economy of alkali liquor use is increased, the discharge of hydrogen in the process is reduced, the economic benefit is increased, the service life of pure water in the water tank is prolonged through the nitrogen-nitrogen sealed water tank, and the pure water can safely and reliably reenter the system for circulation.
Drawings
FIG. 1 is a schematic diagram of the system connection of the present invention;
in the figure: the system comprises a gas-liquid separation module, a 101-gas-alkali separator, a 102-scrubber, a 103-gas cooler, a 104-gas-water separator, a 2-PLC control module, a 201-first switch valve, a 202-second switch valve, a 203-third switch valve, a 3-drying and purifying drainage module, a 4-liquid discharge treatment module, a 401-liquid level meter, a 402-liquid collector 1, 402 a-low liquid level point, a 402 b-high liquid level point, a 5-water replenishing module, a 501-water tank, a 502-water replenishing pump and a 503-back pressure valve.
Detailed Description
The following further describes the embodiments of the present invention with reference to the drawings, and the present embodiment is not to be construed as limiting the invention.
As shown in fig. 1, a system for recycling hydrogen production separation liquid for the second time, including gas-liquid separation module 1, PLC control module 2, dry purification drainer 3, flowing back processing module 4 and moisturizing module 5, the first entry end of gas-liquid separation module 1 lets in the gas-alkali mixture that hydrogen production separation produced, the second entry end of gas-liquid separation module 1 passes through the pipeline intercommunication with the first entry end of flowing back processing module 4, the pipeline intercommunication is crossed with the second entry end of flowing back processing module 4 to the exit end of dry purification drainer 3, the pipeline intercommunication is passed through with the entry end of moisturizing module 5 to the exit end of flowing back processing module 4, the pipeline intercommunication is passed through with the entry end of moisturizing module 5 to the exit end of moisturizing module 5.
The gas-liquid separation module 1 comprises a gas-alkali separator 101, a scrubber 102, a gas cooler 103 and a gas-water separator 104, wherein a gas-alkali mixture generated by hydrogen production separation is introduced into a first water inlet of the gas-alkali separator 101, a second water inlet of the gas-alkali separator 101 is communicated with a water supplementing module 5 through a pipeline, an exhaust port of the gas-alkali separator 101 is communicated with an air inlet of the scrubber 102 through a pipeline, an exhaust port of the scrubber 102 is communicated with an air inlet of the gas cooler 103, an exhaust port of the gas cooler 103 is communicated with an air inlet of the gas-water separator 104 through a pipeline, a water outlet of the gas cooler 103 is communicated with a liquid discharge processing module 4 through a pipeline, and a water outlet of the gas-water separator 104 is communicated with the liquid discharge processing module 4 through a pipeline.
The water supplementing module 5 comprises a water tank 501, a water supplementing pump 502 and a back pressure valve 503, a water inlet of the water tank 501 is communicated with the liquid discharge processing module 4 through a pipeline, an exhaust port of the water tank 501 is communicated with the back pressure valve 503, a water inlet of the water supplementing pump 502 is communicated with a water outlet of the water tank 501, and the water tank 501 is further provided with a nitrogen gas inlet.
The liquid discharge treatment module 4 comprises a liquid level meter 401 and a liquid collector 402, wherein the liquid level meter 401 is arranged in the liquid collector 402, a first water inlet of the liquid collector 402 is communicated with a water outlet of the gas cooler 103 and a water outlet of the gas-water separator 104 through pipelines, a second water inlet of the liquid collector 402 is communicated with a water outlet of the drying and purifying water discharger 3 through a pipeline, and a water outlet of the liquid collector 402 is communicated with a water inlet of the water tank 501 through a pipeline.
A first switch valve 201 is arranged at a first water inlet of the liquid collector 402, a second switch valve 202 is arranged at a water outlet of the liquid collector 402, and a third switch valve 203 is arranged at a nitrogen inlet of the water tank 501.
A high liquid level point 402b and a low liquid level point 402a are arranged in two layers of a liquid level meter 401 in a liquid collector 402, a PLC control module 2 is connected with a first switch valve 201, a second switch valve 202, a third switch valve 203, the liquid level meter 401 and a water replenishing pump 502, and the PLC control module 2 monitors the liquid level conditions of the high liquid level point 402b and the low liquid level point 402a in the liquid collector 402 through the liquid level meter 401 so as to control the opening and closing of the first switch valve 201, the second switch valve 202, the third switch valve 203 and the water replenishing pump 502.
A secondary recycling method of hydrogen production separation liquid comprises the following specific steps:
the gas-alkali mixture generated by the electrolysis of the hydrogen production electrolytic cell enters a gas-alkali separator 101, the temperature in the gas is high at the moment, the content of water vapor and alkali is extremely high, the gas is filtered by a cleaner 102, the alkali content in the gas is reduced, the temperature of the gas is reduced by a cooler 103, water in the gas is condensed into liquid, the water vapor content in the gas is reduced, part of separated liquid water remains in the cooler 103, the separated gas and part of liquid water enter a gas-water separator 104, a first switch valve 201 is opened after a period of time interval by a PLC control module 2, and the liquid water in the cooler 103 and the gas-water separator 104 flows to a liquid collector 401 under the driving of system pressure and gravity.
Water collected by dry purification drainage module 3 passes through bottom pipeline flow direction collector 401, the level gauge 401 monitoring liquid level on collector 401 top, the signal returns to PLC control module 2, when reaching and setting for high liquid level point 402b, open second ooff valve 202 through PLC control module 2 control, flow to moisturizing case 501 under the drive of liquid internal pressure and gravity in the collector 401, when the liquid level is low to low liquid level point 402a, close second ooff valve 202 through PLC control module 2 control, the liquid that the system operation produced at this moment is from newly supplementing to in the water tank 501 after, open moisturizing pump 502 through PLC control module 2 control and mend gas-alkali separator 101 again.
In order to prevent the gas dissolved in the liquid from releasing in the water tank 501 to cause the generation of a mixed gas dangerous source, namely, the mixing of hydrogen and oxygen, and simultaneously ensure that no oxygen exists in the water replenishing tank 501 to prevent the reproduction of aerobic microorganisms in the water, the PLC control module 2 is controlled to periodically open the third switch valve 203 on the water tank 501 to flush nitrogen into the water tank 501 for replacement to form micro-pressure nitrogen protection, the pressure of a micro-pressure system is 50-200kPa, and the replacement gas is discharged through the back pressure valve 503.
While the invention has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted without departing from the spirit and scope of the invention.
Claims (8)
1. The utility model provides a secondary recycle system of hydrogen production separation liquid which characterized in that, includes gas-liquid separation module (1), PLC control module (2), dry purification drainer (3), flowing back processing module (4) and moisturizing module (5), the first entry end of gas-liquid separation module (1) lets in the gas-alkali mixture that the hydrogen production separation produced, the second entry end of gas-liquid separation module (1) passes through the pipeline intercommunication with the first entry end of flowing back processing module (4), the exit end of dry purification drainer (3) and the second entry end of flowing back processing module (4) cross the pipeline intercommunication, the exit end of flowing back processing module (4) passes through the pipeline intercommunication with the entry end of moisturizing module (5), the exit end of moisturizing module (5) passes through the pipeline intercommunication with the entry end of gas-liquid separation module (1).
2. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein the gas-liquid separation module (1) comprises a gas-alkali separator (101), a scrubber (102), a gas cooler (103) and a gas-water separator (104), a first water inlet of the gas-alkali separator (101) is filled with a gas-alkali mixture generated by hydrogen production separation, a second water inlet of the gas-alkali separator (101) is communicated with the water replenishing module (5) through a pipeline, an exhaust port of the gas-alkali separator (101) is communicated with a gas inlet of the scrubber (102) through a pipeline, an exhaust port of the scrubber (102) is communicated with a gas inlet of the gas cooler (103), an exhaust port of the gas cooler (103) is communicated with a gas inlet of the gas-water separator (104) through a pipeline, a water outlet of the gas cooler (103) is communicated with the liquid discharge treatment module (4) through a pipeline, and a water outlet of the gas-water separator (104) is communicated with the liquid discharge treatment module (4) through a pipeline.
3. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein the water replenishing module (5) comprises a water tank (501), a water replenishing pump (502) and a back pressure valve (503), the water inlet of the water tank (501) is communicated with the liquid discharge treatment module (4) through a pipeline, the air outlet of the water tank (501) is communicated with the back pressure valve (503), the water inlet of the water replenishing pump (502) is communicated with the water outlet of the water tank (501), and the water tank (501) is further provided with a nitrogen inlet.
4. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein the liquid discharge treatment module (4) comprises a liquid level meter (401) and a liquid trap (402), the liquid level meter (401) is disposed inside the liquid trap (402), a first water inlet of the liquid trap (402) is communicated with a water outlet of the gas cooler (103) and a water outlet of the gas-water separator (104) through a pipeline, a second water inlet of the liquid trap (402) is communicated with a water outlet of the drying and purifying water trap (3) through a pipeline, and a water outlet of the liquid trap (402) is communicated with a water inlet of the water tank (501) through a pipeline.
5. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein a first switch valve (201) is arranged at a first water inlet of the liquid collector (402), a second switch valve (202) is arranged at a water outlet of the liquid collector (402), and a third switch valve (203) is arranged at a nitrogen inlet of the water tank (501).
6. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein the liquid trap (402) is provided with a high liquid level point (402 b) and a low liquid level point (402 a) in two layers of the liquid level meter (401).
7. The secondary recycling system of the hydrogen production separation liquid according to claim 1, wherein the PLC control module (2) is connected to the first switch valve (201), the second switch valve (202), the third switch valve (203), the liquid level meter (401), and the water replenishing pump (502), and the PLC control module (2) controls the opening and closing of the first switch valve (201), the second switch valve (202), the third switch valve (203), and the water replenishing pump (502) by monitoring the liquid level condition in the liquid collector (402) through the liquid level meter (401).
8. A secondary recycling method of hydrogen production separation liquid is characterized by comprising the following specific steps:
gas-alkali mixture generated by electrolysis of a hydrogen production electrolytic cell enters a gas-alkali separator (101), the temperature in gas is high at the moment, the content of water vapor and alkali is extremely high, the gas is filtered by a cleaner (102) to reduce the alkali content in the gas, the temperature of the gas is reduced by a cooler (103), water in the gas is condensed into liquid to reduce the water vapor content in the gas, part of separated liquid water remains in the cooler (103), the separated gas and part of liquid water enter a gas-water separator (104), a first switch valve (201) is opened after a period of time by a PLC control module (2), and the liquid water in the cooler (103) and the gas-water separator (104) flows to a liquid collector (401) under the drive of system pressure and gravity;
water collected by the drying and purifying drainage module (3) flows to the liquid collector (401) through a bottom pipeline, a liquid level meter (401) at the top end of the liquid collector (401) monitors a liquid level, a signal returns to the PLC control module (2), when a set high liquid level point (402 b) is reached, the PLC control module (2) controls to open the second switch valve (202), the liquid in the liquid collector (401) is driven by pressure and gravity to flow to the water replenishing tank (501), when the liquid level is lowered to a low liquid level point (402 a), the PLC control module (2) controls to close the second switch valve (202), and at the moment, liquid generated by system operation is replenished into the water tank (501) again, and then the PLC control module (2) controls to open the water replenishing pump (502) to replenish the gas-alkali separator (101);
in order to prevent the mixed gas dangerous source caused by the release of gas dissolved in liquid in the water tank (501) and ensure that no oxygen exists in the water supplementing tank (501) and no oxidation reaction occurs in water, the PLC control module (2) is controlled to periodically open a third switch valve (203) on the water tank (501) to flush nitrogen into the water tank (501) for replacement to form micro-pressure nitrogen protection, the pressure of a micro-pressure system is 50-200kPa, and replacement gas is discharged through a back pressure valve (503).
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211012034.3A CN115364632A (en) | 2022-08-23 | 2022-08-23 | Secondary recycling system and method for hydrogen production separation liquid |
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| CN202211012034.3A CN115364632A (en) | 2022-08-23 | 2022-08-23 | Secondary recycling system and method for hydrogen production separation liquid |
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