WO2023071281A1 - 一种氢气纯化系统和方法以及电解水制氢系统 - Google Patents

一种氢气纯化系统和方法以及电解水制氢系统 Download PDF

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WO2023071281A1
WO2023071281A1 PCT/CN2022/103910 CN2022103910W WO2023071281A1 WO 2023071281 A1 WO2023071281 A1 WO 2023071281A1 CN 2022103910 W CN2022103910 W CN 2022103910W WO 2023071281 A1 WO2023071281 A1 WO 2023071281A1
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gas
hydrogen
dryer
opening
heat exchanger
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French (fr)
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郭鲁宁
王高发
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Wuxi Longi Hydrogen Technology Co Ltd
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Wuxi Longi Hydrogen Technology Co Ltd
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Priority to EP22885186.1A priority Critical patent/EP4424635A4/en
Priority to AU2022374739A priority patent/AU2022374739A1/en
Priority to US18/706,181 priority patent/US20250303356A1/en
Publication of WO2023071281A1 publication Critical patent/WO2023071281A1/zh
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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
    • B01D53/261—Drying gases or vapours by adsorption
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0438—Cooling or heating systems
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0462—Temperature swing adsorption
    • 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
    • B01D53/28—Selection of materials for use as drying agents
    • C—CHEMISTRY; METALLURGY
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    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen; Reversible storage of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen-containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • 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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/083—Separating products
    • 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
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/10—Single element gases other than halogens
    • B01D2257/104—Oxygen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B01D2259/40054—Recycled product or process gas treated before its reuse
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/403—Further details for adsorption processes and devices using three beds
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0446—Means for feeding or distributing gases
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0495—Composition of the impurity the impurity being water
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • 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

Definitions

  • the present application relates to the technical field of hydrogen purification, in particular to a hydrogen purification system and method and a hydrogen production system by electrolysis of water.
  • Water electrolysis hydrogen contains trace oxygen and a large amount of water vapor. In order to obtain high-purity hydrogen, water electrolysis hydrogen needs to be purified.
  • Chinese patent CN1920100A discloses a device for continuously purifying water and electrolyzing hydrogen.
  • the device includes 3 drying towers, each of which is equipped with an electric heating rod, which is used to heat the desiccant in the drying tower when regenerating. High-temperature environment; each drying tower is connected to a regeneration cooler, which is used to cool the high-temperature regeneration tail gas generated during the regeneration of the desiccant.
  • the above-mentioned device has many electric heating rods and coolers, and does not make full use of the waste heat of the high-temperature regeneration exhaust gas, so there are problems of high manufacturing cost and energy waste.
  • the purpose of this application is to solve the problems of high manufacturing cost and waste of energy in existing hydrogen purification devices, and provide a hydrogen purification system and method and a hydrogen production system by electrolysis of water.
  • the present application provides a hydrogen purification system for purifying hydrogen to be purified to form purified hydrogen
  • the hydrogen purification system includes:
  • a deoxidation module, a drying module and a regeneration cycle module connected in sequence the drying module includes a first dryer, a second dryer and a third dryer connected in parallel; the regeneration cycle module includes a first gas channel and a second The first gas-gas heat exchanger of the gas channel;
  • the hydrogen purification system also includes:
  • the first gas limiting module is used to allow the hydrogen to be purified to flow through the deoxygenation module and the first dryer to form a purification channel to obtain the purified hydrogen;
  • the second gas limiting module is used to allow part of the purified hydrogen to flow through the first gas channel of the first gas-gas heat exchanger, the second dryer, and the first gas-gas heat exchanger in sequence.
  • the second gas channel and the third dryer form a regeneration channel to obtain recovered hydrogen.
  • the first dryer, the second dryer and the third dryer all have a first opening and a second opening, wherein the first opening of the first dryer, the first The first opening of the second dryer and the first opening of the third dryer can be respectively connected to the outlet of the deoxygenation module, the second gas channel inlet of the first gas-gas heat exchanger, and the first gas channel inlet.
  • the second gas channel outlet of the gas heat exchanger is communicated;
  • the second opening of the first dryer, the second opening of the second dryer and the second opening of the third dryer can be respectively connected with the purified hydrogen
  • the outlet, the first gas channel inlet of the first gas-gas heat exchanger, and the recovered hydrogen outlet are connected;
  • the purified hydrogen outlet is used to output the purified hydrogen
  • the recovered hydrogen outlet is used to output the recovered hydrogen
  • the first air limiting module includes at least one first control valve
  • the second air limiting module includes at least one second control valve
  • the first control valve is arranged between the outlet of the deoxygenation module and the first opening of each dryer and between the purified hydrogen outlet and the second opening of each dryer;
  • the second control valve is arranged between the first gas channel inlet of the first gas-gas heat exchanger and the second opening of each dryer, and between the second gas channel inlet of the first gas-gas heat exchanger and Between the first openings of each dryer, between the second gas channel outlet of the first gas-gas heat exchanger and the first opening of each dryer, and between the recovered hydrogen outlet and the second opening of each dryer between.
  • the regeneration cycle module also includes:
  • a cooler used to lower the temperature of the second dryer
  • the third gas limiting module is used to allow part of the purified hydrogen to flow through the cooler, the second dryer, the second gas channel of the first gas-gas heat exchanger, and the third dryer in sequence , forming a regenerative cooling channel.
  • the inlet of the cooler can communicate with the second opening of the first dryer, the second opening of the second dryer, and the second opening of the third dryer respectively, and the cooling
  • the outlet of the dryer can communicate with the second opening of the first dryer, the second opening of the second dryer and the second opening of the third dryer, respectively.
  • the third air limiting module includes at least one third control valve, and the third control valve is arranged between the inlet of the cooler and the second opening of each dryer, and/or, the cooler between the outlet of each dryer and the second opening of each dryer.
  • the regenerative cycle module further includes a regenerative cooler and a first steam-water separator, the inlet of the regenerative cooler communicates with the outlet of the second gas channel of the first gas-gas heat exchanger, and the regenerative The outlet of the cooler communicates with the inlet of the first steam-water separator, and the outlet of the first steam-water separator can be respectively connected with the first opening of the first dryer and the first opening of the second dryer.
  • the opening or the first opening of the third dryer communicates.
  • the deoxidation module includes a second gas-gas heat exchanger and a deoxidizer, the second gas-gas heat exchanger has a first gas channel and a second gas channel, wherein the second gas-gas heat exchange
  • the outlet of the first gas channel of the device communicates with the inlet of the deaerator
  • the outlet of the deaerator communicates with the inlet of the second gas channel of the second gas-gas heat exchanger
  • the outlet of the second gas-gas heat exchanger The second gas channel outlet can communicate with the first opening of the first dryer, the first opening of the second dryer or the first opening of the third dryer, respectively.
  • the hydrogen purification system further includes a cooling condenser and a second steam-water separator, wherein the inlet of the cooling condenser communicates with the outlet of the second gas channel of the second gas-gas heat exchanger, and the The outlet of the cooling condenser communicates with the inlet of the second steam-water separator, and the outlet of the second steam-water separator can be respectively connected with the first opening of the first dryer and the first opening of the second dryer. Or the first opening of the third dryer communicates.
  • a first condensed water discharge pipe is also provided between the second gas passage inlet of the first gas-gas heat exchanger and the first openings of each dryer, and one end of the first condensed water discharge pipe is simultaneously communicate with the second gas channel inlet of the first gas-gas heat exchanger and the first openings of each dryer;
  • a second condensed water discharge pipe is also provided between the second gas channel inlet of the second gas-gas heat exchanger and the outlet of the deaerator, and the second condensed water discharge pipe is connected with the second gas-gas channel at the same time.
  • the inlet of the second gas channel of the heat exchanger communicates with the outlet of the deaerator;
  • Both the first condensed water discharge pipe and the second condensed water discharge pipe are provided with control valves.
  • a first temperature measuring device is provided on the deoxidizer, a second temperature measuring device is provided at the outlet of the deoxidizer, and a third temperature measuring device is provided at the first opening of the first dryer , the first opening of the second drier is provided with a fourth temperature measuring device, and the first opening of the third drier is provided with a fifth temperature measuring device.
  • the regenerative cycle module also includes a heater
  • the second gas limiting module is specifically used to allow part of the purified hydrogen to flow sequentially through the first gas channel of the first gas-gas heat exchanger, the heater, the second dryer, the The second gas channel of the first gas-gas heat exchanger and the third dryer form a regeneration channel to obtain recovered hydrogen.
  • the second opening of the first dryer, the second opening of the second dryer, and the second opening of the third dryer can also communicate with the outlet of the heater respectively;
  • the outlet of the first gas channel of the first gas-gas heat exchanger communicates with the inlet of the heater.
  • the second control valve is further arranged between the outlet of the heater and the second opening of each dryer.
  • the heater is provided with a sixth temperature measuring device, and the outlet of the heater is provided with a seventh temperature measuring device.
  • the first dryer, the second dryer and the third dryer are all cylindrical structures, and molecular sieve desiccant is arranged in the cylinder.
  • the present application also provides a water electrolysis hydrogen production system
  • the electrolysis water hydrogen production system includes the electrolysis water hydrogen production module and the hydrogen purification system described in any one of the above, the electrolysis water hydrogen production module and the hydrogen purification system
  • the deoxygenation module is connected.
  • the present application also provides a method for purifying hydrogen using the hydrogen purification system described in any one of the above, the method for purifying hydrogen includes:
  • the flow direction of the high-temperature regenerated hydrogen and the gas flow of the deoxygenated hydrogen into the second dryer is opposite.
  • the method for purifying hydrogen further includes: repeating operations S02 to S07, drying the hydrogen after deoxygenation in the second dryer, and drying the unborn molecular sieve in the third dryer The agent is blown and regenerated, and the low-temperature regeneration tail gas is dried in the first dryer; and/or,
  • the method for purifying hydrogen further includes:
  • the hydrogen to be purified enters the deoxygenation module for deoxidation treatment to obtain hydrogen after deoxidation, including:
  • the hydrogen to be purified sequentially enters the first gas channel of the second gas-gas heat exchanger for heat exchange treatment, enters the deoxidizer for deoxidation treatment, and enters the first gas channel of the second gas-gas heat exchanger. performing heat exchange treatment on the hydrogen to be purified in the second gas channel and the first gas channel to obtain the deoxygenated hydrogen.
  • the volume of a part separated from the purified hydrogen accounts for 10-15% of the total volume of the purified hydrogen.
  • the temperature of the deoxidation treatment is 85-100°C; in operation S02, the temperature of the drying treatment is room temperature; in operation S04, the temperature of the drying and regeneration is 250-300°C; In operation S06, the temperature of the drying treatment is room temperature.
  • the method for purifying hydrogen before the deoxygenated hydrogen enters the first dryer, the method for purifying hydrogen further includes:
  • the deoxygenated hydrogen gas is sequentially entered into the cooling condenser for condensation treatment, and then enters the second steam-water separator for steam-water separation treatment.
  • the method for purifying hydrogen before the low-temperature regeneration tail gas enters the third dryer for drying treatment, the method for purifying hydrogen further includes:
  • the low-temperature regeneration tail gas is sequentially entered into the regeneration cooler for condensation treatment, and then enters the first steam-water separator for steam-water separation treatment.
  • the regenerative cycle module also includes a heater
  • the second gas limiting module is specifically used to allow part of the purified hydrogen to flow sequentially through the first gas channel of the first gas-gas heat exchanger, the heater, the second dryer, the The second gas channel and the third dryer of the first gas-to-gas heat exchanger form a regeneration channel to obtain recovered hydrogen;
  • Operation S03 specifically includes:
  • the temperature of the heat treatment is 300-350°C.
  • the three dryers in the hydrogen purification system of the present application share one regeneration cycle module, which significantly reduces the number of regeneration cycle modules, therefore, the manufacturing cost of the system is low; at the same time, the regeneration cycle system is provided with
  • the first gas-gas heat exchanger enables heat exchange between the low-temperature regeneration hydrogen before regeneration and the high-temperature regeneration tail gas after regeneration. On the one hand, it can make full use of the waste heat of the high-temperature regeneration tail gas, and on the other hand, it can significantly reduce subsequent heaters and regeneration.
  • the power consumption of the cooler therefore, the energy consumption of the system is low.
  • Fig. 1 is a structural schematic diagram of the hydrogen purification system of the present application.
  • the first aspect of the present application provides a hydrogen purification system, which is used to purify hydrogen to be purified to form purified hydrogen.
  • the hydrogen purification system may include: a deoxygenation module, a drying module and a regeneration cycle module connected in sequence , the drying module includes a first dryer 1, a second dryer 2 and a third dryer 3 connected in parallel; device 4;
  • the hydrogen purification system also includes: a first gas limiting module, for the hydrogen to be purified to flow through the deoxygenation module and the first dryer 1 in sequence to form a purification channel to obtain the purified hydrogen; a second limiting The gas module is used to allow part of the purified hydrogen to flow through the first gas passage of the first gas-gas heat exchanger 4, the second dryer 2, and the first gas-gas heat exchanger 4 in sequence.
  • the second gas channel and the third dryer 3 form a regeneration channel to obtain recovered hydrogen.
  • the first dryer 1 , the second dryer 2 and the third dryer 3 all have a first opening and a second opening, wherein the first opening of the first dryer 1 , the first opening of the second drier 2 and the first opening of the third drier 3 can be respectively connected to the outlet of the deoxidation module and the second gas passage inlet of the first gas-gas heat exchanger 4 It communicates with the second gas channel outlet of the first gas-gas heat exchanger 4; the second opening of the first dryer 1, the second opening of the second dryer 2 and the third dryer 3
  • the second opening of the second opening can be communicated with the outlet of purified hydrogen, the inlet of the first gas channel of the first gas-gas heat exchanger 4, and the outlet of recovered hydrogen respectively; wherein, the outlet of purified hydrogen is used to output the purified hydrogen,
  • the recovered hydrogen outlet is used to output the recovered hydrogen.
  • each opening (including each outlet and each inlet) can be communicated through a gas delivery pipe, and when multiple openings communicate with the same other opening at the same time, the multiple openings can be independently connected to this The other openings are connected, and multiple openings can also be connected in parallel to each other and then communicate with the other openings through a gas delivery pipeline.
  • the present application preferably connects the multiple openings in parallel with each other and then communicates with the other opening through a gas delivery pipeline.
  • the first opening of the first dryer, the first opening of the second dryer, and the first opening of the third dryer can be connected in parallel, Then communicate with the outlet of the deoxygenation module, the second gas channel inlet of the first gas-gas heat exchanger and the second gas channel outlet of the first gas-gas heat exchanger through different pipelines; the second opening of the first dryer, The second opening of the second dryer and the second opening of the third dryer can also be connected in parallel with each other, and then respectively connected with the outlet of purified hydrogen, the inlet of the first gas passage of the first gas-gas heat exchanger, and the recovery of hydrogen through different pipelines. Export connection.
  • the hydrogen purification system of the present application can be used specifically for the purification of hydrogen from water electrolysis, wherein the deoxygenation module can be used to remove a small amount of oxygen contained in the hydrogen gas from water electrolysis, and the drying module can be used to remove a large amount of water vapor contained in the hydrogen gas from water electrolysis.
  • the regeneration cycle module can be used to heat the cold gas stream before regeneration and cool the hot gas stream after regeneration during desiccant regeneration.
  • the hydrogen purification system of the present application can simultaneously realize the purification treatment of the hydrogen to be purified, the regeneration treatment of the desiccant to be produced in the dryer, and the recovery treatment of the regeneration tail gas.
  • any dryer can be used to purify the hydrogen to be purified At the same time, regenerate the desiccant in another drier, and use the remaining drier to dry and recover the regenerated tail gas.
  • the hydrogen to be purified can first enter the deoxidation module for deoxidation treatment to obtain hydrogen after deoxygenation; then the hydrogen after deoxygenation can enter the dryer from the first opening of any dryer Drying treatment is carried out in the middle to obtain purified hydrogen, and a part of the purified hydrogen is separated as low-temperature regenerated hydrogen from the first gas channel inlet of the first gas-gas heat exchanger into the first gas channel of the first gas-gas heat exchanger for exchange.
  • the above-mentioned operation processes can be carried out in turn in each dryer, so as to realize the continuous purification of the hydrogen to be purified.
  • the hydrogen after deoxidation can be dried in the first dryer, and the molecular sieve to be purified in the second dryer can be dried.
  • the desiccant is blown and regenerated, and the low-temperature regeneration tail gas is dried in the first dryer; then, the hydrogen after deoxygenation is dried in the second dryer, and the desiccant molecular sieve desiccant in the third dryer is dried.
  • Blow-dry regeneration dry the low-temperature regeneration tail gas in the first dryer; finally, dry the deoxygenated hydrogen in the third dryer, and blow-dry and regenerate the molecular sieve desiccant in the first dryer , and dry the low-temperature regeneration tail gas in the second dryer.
  • a closed-loop circulation process is formed, thereby realizing continuous purification of the hydrogen to be purified.
  • the three dryers in the hydrogen purification system share one regeneration cycle module, which significantly reduces the number of regeneration cycle modules. Therefore, the manufacturing cost of the system is low; at the same time, the regeneration cycle system is provided with a first gas
  • the gas heat exchanger enables heat exchange between the low-temperature regeneration hydrogen before regeneration and the high-temperature regeneration tail gas after regeneration. On the one hand, it can make full use of the waste heat of the high-temperature regeneration tail gas, and on the other hand, it can significantly reduce the subsequent heater and regeneration cooler. power consumption, therefore, the power consumption of the system is low.
  • the first air limiting module may include at least one first control valve
  • the second air limiting module may include at least one second control valve
  • the first control valve may be arranged in the deoxygenation module Between the outlet and the first opening of each dryer and between the outlet of the purified hydrogen and the second opening of each dryer
  • the second control valve can be arranged at the first Between the gas channel inlet and the second opening of each dryer, between the second gas channel inlet of the first gas-gas heat exchanger 4 and the first opening of each dryer, the first gas-gas heat exchanger Between the outlet of the second gas channel of 4 and the first opening of each dryer, and between the hydrogen recovery outlet and the second opening of each dryer.
  • the types of the first control valve and the second control valve can be selected within a certain range, for example, they can be pneumatic ball valves.
  • the switching of the flow paths between the openings can be realized to prevent the air flow from entering other flow paths, for example, by opening the connection between the outlet of the deoxidation module and the first opening of the first dryer and close the first control valve between the outlet of the deoxidation module and the first opening of the second dryer and the first opening of the third dryer to open the flow path between the deoxidation module and the first dryer , closing the flow path between the deoxygenation module and the second dryer and the third dryer, so that the deoxygenated hydrogen enters the first dryer but does not enter the second dryer and the third dryer.
  • the regenerative cycle module also includes a heater 5;
  • the second gas limiting module is specifically used to allow part of the purified hydrogen to flow sequentially through the first gas channel of the first gas-gas heat exchanger 4, the heater 5, the second dryer 2,
  • the second gas channel of the first gas-gas heat exchanger 4 and the third dryer 3 form a regeneration channel to obtain recovered hydrogen.
  • the three dryers in the hydrogen purification system share a regeneration cycle module, and the regeneration cycle module includes a heater, so the application significantly reduces the number of heaters, and the manufacturing cost of the system is relatively low; at the same time, the regeneration cycle
  • the system is equipped with a first gas-gas heat exchanger, so that the low-temperature regeneration hydrogen before regeneration can exchange heat with the high-temperature regeneration tail gas after regeneration.
  • the waste heat of the high-temperature regeneration tail gas can be fully utilized, and on the other hand, the subsequent The power consumption of the heater and regenerative cooler, therefore, the energy consumption of the system is low.
  • the second opening of the first dryer 1, the second opening of the second dryer 2 and the second opening of the third dryer 3 can also communicate with the outlet of the heater 5 respectively;
  • the outlet of the first gas passage of the device 4 communicates with the inlet of the heater 5 .
  • a part of the purified hydrogen is separated as low-temperature regenerated hydrogen from the first gas channel inlet of the first gas-gas heat exchanger into the first gas channel of the first gas-gas heat exchanger for heat exchange treatment, and then passed through the first gas
  • the outlet of the first gas channel of the gas heat exchanger and the inlet of the heater enter the heater for heat treatment to obtain high-temperature regenerated hydrogen.
  • the second control valve is also arranged between the outlet of the heater 5 and the second opening of each dryer.
  • a sixth temperature measuring device 21 may be provided on the heater 5
  • a seventh temperature measuring device 22 may be provided at the outlet of the heater 5 .
  • the regeneration cycle module may further include: a cooler 8 for cooling down the second dryer 2; a third gas limiting module for allowing part of the purified hydrogen to sequentially flow through the cooling
  • the device 8, the second dryer 2, the second gas channel of the first gas-gas heat exchanger 4 and the third dryer 3 form a regenerative cooling channel.
  • the inlet of the cooler 8 can communicate with the second opening of the first dryer 1, the second opening of the second dryer 2 and the second opening of the third dryer 3 respectively, so The outlet of the cooler 8 can communicate with the second opening of the first dryer 1 , the second opening of the second dryer 2 and the second opening of the third dryer 3 respectively.
  • the three dryers in the hydrogen purification system share one regenerative cycle module, and the regenerative cycle module includes heaters and coolers, so this application significantly reduces the number of heaters and coolers, and the manufacturing cost of the system is relatively low. Low.
  • the type of the cooler 8 can be selected within a certain range, for example, it can be a blown cooler, which is mainly used for drying the hydrogen from the hydrogen to be purified after a period of regeneration of the desiccant. Part of the purified hydrogen of the desiccant is cooled, and this part of the purified hydrogen after the cooling treatment enters the desiccant regeneration dryer to quickly cool the regenerated high-temperature regenerated desiccant. On the one hand, the regeneration process can be shortened On the other hand, it can keep the regenerated desiccant in a low temperature state and increase its adsorption capacity.
  • the regeneration process of the standby desiccant in the system of this application includes at least two operations.
  • the first operation is to use the high-temperature regenerated hydrogen heated by the first gas-gas heat exchanger and heater to take away the standby desiccant.
  • the second operation is to use the low-temperature purified hydrogen cooled by the cooler to quickly cool the high-temperature regenerated desiccant obtained after the first operation.
  • the third air limiting module may include at least one third control valve, and the third control valve may be arranged between the inlet of the cooler 8 and the second opening of each dryer, and/or, the Between the outlet of the cooler 8 and the second opening of each dryer.
  • the third control valve Through the regulation of the third control valve, part of the purified hydrogen from the drier used for drying the hydrogen to be purified can flow to the cooler 8 instead of flowing to the first gas channel of the first gas-gas heat exchanger 4 .
  • the regenerative cycle module may also include a regenerative cooler 6 and a first steam-water separator 7, the inlet of the regenerative cooler 6 is connected to the outlet of the second gas channel of the first gas-gas heat exchanger 4
  • the outlet of the regenerative cooler 6 communicates with the inlet of the first steam-water separator 7, and the outlet of the first steam-water separator 7 can be respectively connected with the first opening of the first dryer 1, The first opening of the second dryer 2 or the first opening of the third dryer 3 communicates.
  • the deoxidation module may further include a second gas-gas heat exchanger 10 and a deoxidizer 11, the second gas-gas heat exchanger 10 has a first gas channel and a second gas channel, wherein the first The first gas channel outlet of the second gas-gas heat exchanger 10 is communicated with the inlet of the deoxidizer 11, and the outlet of the deoxidizer 11 is communicated with the second gas channel inlet of the second gas-gas heat exchanger 10, so The second gas channel outlet of the second gas-gas heat exchanger 10 can be connected to the first opening of the first dryer 1, the first opening of the second dryer 2 and the first opening of the third dryer 3 respectively. The first opening communicates.
  • the hot hydrogen gas flow after deoxidation in the deoxidizer can flow back into the second gas channel of the second gas-gas heat exchanger, and flow through
  • the low-temperature hydrogen to be purified in the first gas channel is heated by heat exchange, so that the temperature of the hydrogen to be purified increases, and the temperature of the hydrogen after deoxygenation decreases, which can effectively reduce the power consumption of the deoxidizer and subsequent cooling condenser.
  • the hydrogen purification system may also include a cooling condenser 12 and a second steam-water separator 13, wherein the inlet of the cooling condenser 12 is connected to the second gas channel of the second gas-gas heat exchanger 10 The outlet is communicated, the outlet of the cooling condenser 12 is communicated with the inlet of the second steam-water separator 13, and the outlet of the second steam-water separator 13 can be connected with the first opening of the first dryer 1, the The first opening of the second dryer 2 communicates with the first opening of the third dryer 3 .
  • a first condensed water discharge pipe 14 may also be provided between the second gas channel inlet of the first air-gas heat exchanger 4 and the first openings of each dryer, and the first condensed water discharge pipe 14 One end of 14 communicates with the second gas channel inlet of the first gas-gas heat exchanger 4 and the first opening of each dryer at the same time; the second gas channel inlet of the second gas-gas heat exchanger 10 is connected with the A second condensed water discharge pipe 15 may also be arranged between the outlets of the deaerator 11, and the second condensed water discharge pipe 15 is simultaneously connected with the second gas channel inlet of the second gas-gas heat exchanger 10 and the deoxidizer. The outlet of device 11 is connected. Both the first condensed water discharge pipe and the second condensed water discharge pipe are used to discharge the condensed water accumulated in the gas flow path, so as to prevent the condensed water from entering the air-gas heat exchanger and affecting the heat exchange effect.
  • both the first condensed water discharge pipe 14 and the second condensed water discharge pipe 15 may be provided with control valves.
  • a first temperature measuring device 16 may be provided on the deaerator 11, a second temperature measuring device 17 may be provided at the outlet of the deaerator 11, and a second temperature measuring device 17 may be provided at the first opening of the first dryer 1.
  • a third temperature measuring device 18 may be provided, a fourth temperature measuring device 19 may be provided at the first opening of the second dryer 2, and a fifth temperature measuring device 19 may be provided at the first opening of the third dryer 3.
  • Temperature equipment 20 may be provided on the deaerator 11
  • a second temperature measuring device 17 may be provided at the outlet of the deaerator 11
  • a second temperature measuring device 17 may be provided at the first opening of the first dryer 1.
  • a third temperature measuring device 18 may be provided
  • a fourth temperature measuring device 19 may be provided at the first opening of the second dryer 2
  • a fifth temperature measuring device 19 may be provided at the first opening of the third dryer 3.
  • the first dryer 1 , the second dryer 2 and the third dryer 3 are all in a cylindrical structure, and a molecular sieve desiccant is arranged inside the cylinder. Since each dryer in the system of the present application shares an air-air heat exchanger and heater, there is no need to install electric heating equipment in each dryer, and the effect of energy saving and emission reduction is obvious.
  • the second aspect of the present application provides a hydrogen production system by electrolysis of water.
  • the hydrogen production system by electrolysis of water may include a hydrogen production module by electrolysis of water and the hydrogen purification system described in any one of the above.
  • the deoxygenation module of the hydrogen purification system is connected.
  • a third aspect of the present application provides a method for purifying hydrogen using any one of the systems described above, the method may include operation S01 to operation S07.
  • the hydrogen to be purified enters the deoxidation module for deoxidation treatment to obtain deoxidized hydrogen.
  • the hydrogen gas to be purified may be, for example, water electrolysis hydrogen gas.
  • the deoxidized hydrogen gas enters the first dryer for drying treatment to obtain the purified hydrogen gas.
  • a part of the purified hydrogen is separated as low-temperature regenerated hydrogen into the first gas channel of the first gas-to-gas heat exchanger for heat exchange treatment to obtain high-temperature regenerated hydrogen.
  • the high-temperature regenerated tail gas enters the second gas passage of the first gas-to-gas heat exchanger, and performs heat exchange treatment with the low-temperature regenerated hydrogen in the first gas passage, to obtain Low temperature regeneration exhaust gas.
  • the low-temperature regeneration tail gas enters the third dryer for drying treatment to obtain recovered hydrogen.
  • the recovered hydrogen is combined with the purified hydrogen.
  • the hydrogen purification method may further include: repeating operations S02 to S07, drying the deoxidized hydrogen in the second drier, and drying the molecular sieve to be grown in the third drier
  • the desiccant is blown and regenerated, and the low-temperature regeneration tail gas is dried in the first drier; and/or, operations S02 to S07 are repeated, and the deoxidized hydrogen is deoxidized in the third drier. Drying treatment, drying and regenerating the molecular sieve desiccant in the first dryer, and drying the low-temperature regeneration tail gas in the second dryer.
  • the hydrogen purification method may further include operations S04-1 and Operation S04-2.
  • operation S04-1 stop the low-temperature regenerated hydrogen in operation S03 from entering the first gas channel of the first gas-gas heat exchanger, and let a part of the purified hydrogen enter the cooler for further Cooling treatment, get blown cold hydrogen.
  • operation S04-2 stop making the high-temperature regenerated hydrogen in operation S04 enter the second dryer, and let the blown cold hydrogen enter the second dryer, and dry the second dryer
  • the regenerated molecular sieve desiccant in the device is blown and cooled, and the generated gas replaces the high-temperature regeneration tail gas in operation S05, and continues to perform operations S05-S07, wherein the gas flow direction of the blown-cooled hydrogen gas is in line with the high-temperature regeneration hydrogen gas in the The gas flow direction in the second dryer is the same.
  • the making the hydrogen to be purified enter the deoxidation module for deoxidation treatment to obtain the hydrogen after deoxygenation may include: making the hydrogen to be purified enter the second gas-gas heat exchange sequentially heat exchange treatment in the first gas channel of the deoxidizer, enter the deoxidizer for deoxidation treatment, enter the second gas channel of the second gas-gas heat exchanger and the waiting gas in the first gas channel
  • the purified hydrogen is subjected to heat exchange treatment to obtain the deoxidized hydrogen.
  • the volume of a part separated from the purified hydrogen may account for 10-15% of the total volume of the purified hydrogen.
  • the temperature of the deoxidation treatment may be 85-100°C; in operation S02, the temperature of the drying treatment may be room temperature; in operation S04, the temperature of the drying and regeneration may be 250- 300°C; in operation S06, the temperature of the drying treatment may be room temperature.
  • the method for purifying hydrogen further includes: sequentially entering the deoxidized hydrogen into the cooling condenser for condensation processing, and enter the second steam-water separator for steam-water separation treatment.
  • the method for purifying hydrogen further includes: making the low-temperature regeneration tail gas sequentially enter the regeneration cooler Condensation treatment is carried out in the first steam-water separator, and steam-water separation treatment is carried out in the first steam-water separator.
  • the regenerative cycle module further includes a heater
  • the second gas limiting module is specifically used to allow part of the purified hydrogen to flow sequentially through the first gas channel of the first gas-gas heat exchanger, the heater, the second dryer, the The second gas channel and the third dryer of the first gas-to-gas heat exchanger form a regeneration channel to obtain recovered hydrogen;
  • Operation S03 specifically includes:
  • the temperature of the heat treatment is 300-350°C.
  • step (4) After the dry regeneration in step (4), stop making the low-temperature regenerated hydrogen in step (3) enter the first gas channel of the first gas-gas heat exchanger, and allow a part of the purified hydrogen to enter the cooler Carry out cooling treatment in, obtain blowing cold hydrogen; Stop making the high-temperature regenerated hydrogen in step (4) enter in the second drier, and, make blowing cold hydrogen enter in the second drier, to the regenerated molecular sieve in the second drier The desiccant is blown and cooled to obtain hydrogen after blowing and cooled, and then proceeds to step (6);
  • step (6) make the high-temperature regenerated tail gas that step (4) obtains or the blown hydrogen that step (5) obtains enter in the second gas channel of the first gas-gas heat exchanger and the first gas of the first gas-gas heat exchanger
  • the low-temperature regenerated hydrogen in the channel is subjected to heat exchange treatment, and then flows through the regenerated cooler and the first steam-water separator in sequence to obtain low-temperature regenerated tail gas;
  • steps (2) to (7) After the operation of steps (2) to (7) lasts for 24 hours, transfer the operations related to the dryer in steps (2) and (3) to the second dryer, and transfer steps (4) to (6) ) in the operation related to the drier is transferred to the third drier, and the operation related to the drier in step (7) is transferred to the first drier;

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Abstract

一种氢气纯化系统和方法以及电解水制氢系统，氢气纯化系统中包括三台干燥器，且三台干燥器共用一个再生循环模块，显著减少了再生循环模块的数量，因此系统的制造成本较低；同时，再生循环系统中设置有第一气气换热器（4），使得再生前的低温再生氢气与再生后的高温再生尾气能够进行热量交换，一方面能够充分利用高温再生尾气的余热，另一方面能够显著减少后续加热器和再生冷却器的功耗，因此系统的能耗较低。

Description

一种氢气纯化系统和方法以及电解水制氢系统
本申请要求在2021年10月30日提交中国专利局、申请号为202111277993.3、名称为“一种氢气纯化系统和方法以及电解水制氢系统”的中国专利申请的优先权，其全部内容通过引用结合在本申请中。
技术领域
本申请涉及氢气纯化技术领域，具体涉及一种氢气纯化系统和方法以及电解水制氢系统。
背景技术
水电解氢气中含有微量氧和大量水汽，为了获得高纯度的氢气，需要对水电解氢气进行纯化处理。
中国专利CN1920100A公开了一种连续纯化水电解氢气的装置，该装置包括3座干燥塔，每座干燥塔内均设有电加热棒，用于在对干燥塔内的干燥剂进行再生时加热营造高温环境；每座干燥塔外均分别连接一个再生冷却器，用于对干燥剂再生过程中产生的高温再生尾气进行冷却。
上述装置中具有较多的电加热棒和冷却器，且没有对高温再生尾气的余热进行充分利用，因此存在制造成本较高且能源浪费的问题。
发明内容
本申请的目的是解决现有氢气纯化装置中存在的制造成本较高且能源浪费的问题，提供一种氢气纯化系统和方法以及电解水制氢系统。
为了实现上述目的，本申请提供一种氢气纯化系统，用于对待纯化氢气进行纯化形成提纯氢气，所述氢气纯化系统包括：
依次连通的脱氧模块、干燥模块和再生循环模块，所述干燥模块包括并联连接的第一干燥器、第二干燥器和第三干燥器；所述再生循环模块包括具有第一气体通道和第二气体通道的第一气气换热器；
所述氢气纯化系统还包括：
第一限气模块，用于供所述待纯化氢气依次流经所述脱氧模块和所述第一干燥器形成纯化通道，获得所述提纯氢气；
第二限气模块，用于供部分所述提纯氢气依次流经第一气气换热器的所 述第一气体通道、所述第二干燥器、所述第一气气换热器的第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气。
可选地，所述第一干燥器、所述第二干燥器和所述第三干燥器均具有第一开口和第二开口，其中，所述第一干燥器的第一开口、所述第二干燥器的第一开口和所述第三干燥器的第一开口能够各自分别与所述脱氧模块的出口、所述第一气气换热器的第二气体通道入口和所述第一气气换热器的第二气体通道出口连通；所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口能够各自分别与提纯氢气出口、所述第一气气换热器的第一气体通道入口以及回收氢气出口连通；
其中，所述提纯氢气出口用于输出所述提纯氢气，所述回收氢气出口用于输出所述回收氢气。
可选地，所述第一限气模块包括至少一个第一控制阀，所述第二限气模块包括至少一个第二控制阀；
所述第一控制阀设置在所述脱氧模块的出口与各干燥器的第一开口之间以及所述提纯氢气出口与各干燥器的第二开口之间；
所述第二控制阀设置在所述第一气气换热器的第一气体通道入口与各干燥器的第二开口之间、所述第一气气换热器的第二气体通道入口与各干燥器的第一开口之间、所述第一气气换热器的第二气体通道出口与各干燥器的第一开口之间以及所述回收氢气出口与各干燥器的第二开口之间。
可选地，所述再生循环模块还包括：
冷却器，用于对所述第二干燥器进行降温；
第三限气模块，用于供部分所述提纯氢气依次流经所述冷却器、所述第二干燥器、所述第一气气换热器的第二气体通道和所述第三干燥器，形成再生冷却通道。
可选地，所述冷却器的入口能够分别与所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口连通，所述冷却器的出口能够分别与所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口连通。
可选地，所述第三限气模块包括至少一个第三控制阀，第三控制阀设置在所述冷却器的入口与各干燥器的第二开口之间，和/或，所述冷却器的出口与各干燥器的第二开口之间。
可选地，所述再生循环模块还包括再生冷却器和第一汽水分离器，所述 再生冷却器的入口与所述第一气气换热器的第二气体通道出口连通，所述再生冷却器的出口与所述第一汽水分离器的入口连通，所述第一汽水分离器的出口能够分别与所述第一干燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
可选地，所述脱氧模块包括第二气气换热器和脱氧器，所述第二气气换热器具有第一气体通道和第二气体通道，其中，所述第二气气换热器的第一气体通道出口与所述脱氧器的入口连通，所述脱氧器的出口与所述第二气气换热器的第二气体通道入口连通，所述第二气气换热器的第二气体通道出口能够分别与所述第一干燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
可选地，所述氢气纯化系统还包括冷却冷凝器和第二汽水分离器，其中，所述冷却冷凝器的入口与所述第二气气换热器的第二气体通道出口连通，所述冷却冷凝器的出口与所述第二汽水分离器的入口连通，所述第二汽水分离器的出口能够分别与所述第一干燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
可选地，所述第一气气换热器的第二气体通道入口与各干燥器的第一开口之间还设置有第一冷凝水排放管道，所述第一冷凝水排放管道的一端同时与所述第一气气换热器的第二气体通道入口和各干燥器的第一开口连通；
所述第二气气换热器的第二气体通道入口与所述脱氧器的出口之间还设置有第二冷凝水排放管道，所述第二冷凝水排放管道同时与所述第二气气换热器的第二气体通道入口和所述脱氧器的出口连通；
所述第一冷凝水排放管道和所述第二冷凝水排放管道上均设有控制阀。
可选地，所述脱氧器上设有第一测温设备，所述脱氧器的出口处设有第二测温设备，所述第一干燥器的第一开口处设有第三测温设备，所述第二干燥器的第一开口处设有第四测温设备，所述第三干燥器的第一开口处设有第五测温设备。
可选地，所述再生循环模块还包括加热器；
所述第二限气模块，具体用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述加热器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气。
可选地，所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口还能够分别与所述加热器的出口连通；所述第一气气换热器的第一气体通道出口与所述加热器的入口连通。
可选地，所述第二控制阀还设置所述加热器的出口与各干燥器的第二开口之间。
可选地，所述加热器上设有第六测温设备，所述加热器的出口处设有第七测温设备。
可选地，所述第一干燥器、所述第二干燥器和所述第三干燥器均为筒状结构，筒内设有分子筛干燥剂。
本申请还提供一种电解水制氢系统，所述电解水制氢系统包括电解水制氢模块和上述任意一项所述的氢气纯化系统，所述电解水制氢模块与所述氢气纯化系统的所述脱氧模块连通。
本申请还提供一种利用上述任意一项所述的氢气纯化系统来纯化氢气的方法，所述纯化氢气的方法包括：
S01.使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气；
S02.使所述脱氧后氢气进入所述第一干燥器中进行干燥处理，得到所述提纯氢气；
S03.将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，得到高温再生氢气；
S04.停止向所述第二干燥器中通入所述脱氧后氢气，并使所述高温再生氢气进入所述第二干燥器中，对所述第二干燥器中的待生分子筛干燥剂进行吹干再生，得到高温再生尾气；
S05.使所述高温再生尾气进入所述第一气气换热器的所述第二气体通道中，与所述第一气体通道中的所述低温再生氢气进行换热处理，得到低温再生尾气；
S06.使所述低温再生尾气进入所述第三干燥器中进行干燥处理，得到回收氢气；
S07.使所述回收氢气与所述提纯氢气合并。
可选地，操作S04中，所述高温再生氢气与所述脱氧后氢气通入所述第二干燥器中的气体流向相反。
可选地，所述纯化氢气的方法还包括：重复操作S02～S07，在所述第二干燥器中对所述脱氧后氢气进行干燥处理，对所述第三干燥器中的待生分子筛干燥剂进行吹干再生，在所述第一干燥器中对所述低温再生尾气进行干燥处理；和/或，
重复操作S02～S07，在所述第三干燥器中对所述脱氧后氢气进行干燥处理，对所述第一干燥器中的待生分子筛干燥剂进行吹干再生，在所述第二干燥器中对所述低温再生尾气进行干燥处理。
可选地，在操作S04中利用所述高温再生氢气对所述第二干燥器中的分子筛干燥剂进行吹干再生预设时长后，所述纯化氢气的方法还包括：
S04-1.停止使操作S03中的所述低温再生氢气进入所述第一气气换热器的第一气体通道中，以及，使一部分所述提纯氢气进入所述冷却器中进行冷却处理，得到吹冷氢气；
S04-2.停止使操作S04中的所述高温再生氢气进入所述第二干燥器中，以及，使所述吹冷氢气进入所述第二干燥器中，对所述第二干燥器中的再生分子筛干燥剂进行吹冷处理，所产生气体替换操作S05中的所述高温再生尾气，继续执行操作S05～S07，其中，所述吹冷氢气的气体流向与所述高温再生氢气在所述第二干燥器中的气体流向相同。
可选地，操作S01中，使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气，包括：
使所述待纯化氢气依次进入所述第二气气换热器的第一气体通道中进行换热处理，进入所述脱氧器中进行脱氧处理，进入所述第二气气换热器的第二气体通道中与所述第一气体通道中的所述待纯化氢气进行换热处理，得到所述脱氧后氢气。
可选地，操作S03中，从所述提纯氢气中分出的一部分的体积占所述提纯氢气总体积的10～15％。
可选地，操作S01中，所述脱氧处理的温度为85～100℃；操作S02中，所述干燥处理的温度为室温；操作S04中，所述吹干再生的温度为250～300℃；操作S06中，所述干燥处理的温度为室温。
可选地，操作S02中，在使所述脱氧后氢气进入所述第一干燥器中之前，所述纯化氢气的方法还包括：
使所述脱氧后氢气依次进入所述冷却冷凝器中进行冷凝处理，进入所述第二汽水分离器中进行汽水分离处理。
可选地，操作S06中，在使所述低温再生尾气进入所述第三干燥器中进行干燥处理之前，所述纯化氢气的方法还包括：
使所述低温再生尾气依次进入所述再生冷却器中进行冷凝处理，进入所述第一汽水分离器中进行汽水分离处理。
可选地，所述再生循环模块还包括加热器；
所述第二限气模块，具体用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述加热器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气；
操作S03具体包括：
将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，然后进入所述加热器中进行加热处理，得到所述高温再生氢气。
可选地，操作S03中，所述加热处理的温度为300～350℃。
通过上述技术方案，本申请的氢气纯化系统中的三台干燥器共用一个再生循环模块，显著减少了再生循环模块的数量，因此，该系统的制造成本较低；同时，再生循环系统中设置有第一气气换热器，使得再生前的低温再生氢气与再生后的高温再生尾气能够进行热量交换，这一方面能够充分利用高温再生尾气的余热，另一方面能够显著减少后续加热器和再生冷却器的功耗，因此，该系统的能耗较低。
本申请的其他特征和优点将在随后的具体实施方式部分予以详细说明。
附图说明
附图是用来提供对本申请的进一步理解，并且构成说明书的一部分，与下面的具体实施方式一起用于解释本申请，但并不构成对本申请的限制。在附图中：
图1是本申请的氢气纯化系统的结构示意图。
附图标记说明
1   第一干燥器                2   第二干燥器
3   第三干燥器                4   第一气气换热器
5   加热器                    6   再生冷却器
7   第一汽水分离器            8   冷却器
9   第三汽水分离器            10     第二气气换热器
11     脱氧器                   12     冷却冷凝器
13  第二汽水分离器            14     第一冷凝水排放管道
15  第二冷凝水排放管道        16     第一测温设备
17  第二测温设备              18     第三测温设备
19  第四测温设备              20     第五测温设备
21  第六测温设备              22     第七测温设备
具体实施例
以下结合附图对本申请的具体实施方式进行详细说明。应当理解的是，此处所描述的具体实施方式仅用于说明和解释本申请，并不用于限制本申请。
本申请的第一方面提供一种氢气纯化系统，用于对待纯化氢气进行纯化形成提纯氢气，如图1所示，所述氢气纯化系统可以包括：依次连通的脱氧模块、干燥模块和再生循环模块，所述干燥模块包括并联连接的第一干燥器1、第二干燥器2和第三干燥器3；所述再生循环模块包括具有第一气体通道和第二气体通道的第一气气换热器4；
所述氢气纯化系统还包括：第一限气模块，用于供所述待纯化氢气依次流经所述脱氧模块和所述第一干燥器1形成纯化通道，获得所述提纯氢气；第二限气模块，用于供部分所述提纯氢气依次流经第一气气换热器4的所述第一气体通道、所述第二干燥器2、所述第一气气换热器4的第二气体通道和所述第三干燥器3，形成再生通道，获得回收氢气。
根据本申请，所述第一干燥器1、所述第二干燥器2和所述第三干燥器3均具有第一开口和第二开口，其中，所述第一干燥器1的第一开口、所述第二干燥器2的第一开口和所述第三干燥器3的第一开口能够分别与所述脱氧模块的出口、所述第一气气换热器4的第二气体通道入口和所述第一气气换热器4的第二气体通道出口连通；所述第一干燥器1的第二开口、所述第二干燥器2的第二开口和所述第三干燥器3的第二开口能够分别与提纯氢气出口、所述第一气气换热器4的所述第一气体通道入口以及回收氢气出口连 通；其中，所述提纯氢气出口用于输出所述提纯氢气，所述回收氢气出口用于输出所述回收氢气。
在本申请中，具体地，各开口(包括各出口和各入口)之间可以通过气体输送管道进行连通，当多个开口同时与同一个其他开口连通时，多个开口可以分别独立地与该其他开口连通，多个开口也可以互相并联后再通过一根气体输送管道与该其他开口连通。为了节约系统的制造成本同时简化系统的复杂程度，当多个开口同时与同一个其他开口连通时，本申请优选多个开口互相并联后再通过一根气体输送管道与该其他开口连通。
示例性地，如图1所示，在本申请的氢气纯化系统中，第一干燥器的第一开口、第二干燥器的第一开口和第三干燥器的第一开口可以互相并联后，再通过不同的管道分别与脱氧模块的出口、第一气气换热器的第二气体通道入口和第一气气换热器的第二气体通道出口连通；第一干燥器的第二开口、第二干燥器的第二开口和第三干燥器的第二开口也可以互相并联后，再通过不同的管道分别与提纯氢气出口、第一气气换热器的第一气体通道入口以及回收氢气出口连通。
本申请的氢气纯化系统具体可以用于进行水电解氢气的纯化，其中，脱氧模块可以用于除去水电解氢气中含有的少量氧，干燥模块可以用于除去水电解氢气中含有的大量的水汽，再生循环模块可以用于在干燥剂的再生过程中加热再生之前的冷气流并冷却再生之后的热气流。
本申请的氢气纯化系统能够同时实现对待纯化氢气的纯化处理、对干燥器中待生干燥剂的再生处理以及对再生尾气的回收处理，具体地，可以利用任意一个干燥器对待纯化氢气进行纯化处理，同时对另一个干燥器中的待生干燥剂进行再生处理，并利用剩余干燥器对再生尾气进行干燥回收处理。
具体地，本申请的氢气纯化系统在运行时，可以先使待纯化氢气进入脱氧模块中进行脱氧处理，得到脱氧后氢气；再使脱氧后氢气从任一干燥器的第一开口进入该干燥器中进行干燥处理，得到提纯氢气，并将提纯氢气分出一部分作为低温再生氢气从第一气气换热器的第一气体通道入口进入第一气气换热器的第一气体通道中进行换热处理，得到高温再生氢气；然后，使高温再生氢气从另一干燥器的第二开口进入该干燥器中，对该干燥器中的待生分子筛干燥剂进行吹干再生，得到高温再生尾气，并使得到的高温再生尾气从该干燥器的第一开口流出后，再从第一气气换热器的第二气体通道入口流入第一气气换热器的第二气体通道中与第一气气换热器的第一气体通道 中的低温再生氢气进行换热处理，再经第一气气换热器的第二气体通道出口流出，得到低温再生尾气；接下来，使低温再生尾气从剩余干燥器的第一开口流入该干燥器中进行干燥处理后从该干燥器的第二开口流出，得到回收氢气，并使回收氢气从回收氢气出口流出；最后，使从提纯氢气出口流出的提纯氢气和从回收氢气出口流出的回收氢气合并，得到纯化后氢气。
可以在各干燥器中轮流执行上述各操作过程，从而实现对待纯化氢气的连续纯化，例如，可以先在第一干燥器中对脱氧后氢气进行干燥处理，对第二干燥器中的待生分子筛干燥剂进行吹干再生，在第一干燥器中对低温再生尾气进行干燥处理；然后，在第二干燥器中对脱氧后氢气进行干燥处理，对第三干燥器中的待生分子筛干燥剂进行吹干再生，在第一干燥器中对低温再生尾气进行干燥处理；最后，在第三干燥器中对脱氧后氢气进行干燥处理，对第一干燥器中的待生分子筛干燥剂进行吹干再生，在第二干燥器中对低温再生尾气进行干燥处理。以此形成一个闭环循环过程，从而实现对待纯化氢气的连续纯化。
在本申请中，氢气纯化系统中的三台干燥器共用一个再生循环模块，显著减少了再生循环模块的数量，因此，该系统的制造成本较低；同时，再生循环系统中设置有第一气气换热器，使得再生前的低温再生氢气与再生后的高温再生尾气能够进行热量交换，这一方面能够充分利用高温再生尾气的余热，另一方面能够显著减少后续加热器和再生冷却器的功耗，因此，该系统的能耗较低。
根据本申请，所述第一限气模块可以包括至少一个第一控制阀，所述第二限气模块可以包括至少一个第二控制阀；所述第一控制阀可以设置在所述脱氧模块的出口与各干燥器的第一开口之间以及所述提纯氢气出口与各干燥器的第二开口之间；所述第二控制阀可以设置在所述第一气气换热器4的第一气体通道入口与各干燥器的第二开口之间、所述第一气气换热器4的第二气体通道入口与各干燥器的第一开口之间、所述第一气气换热器4的第二气体通道出口与各干燥器的第一开口之间以及所述回收氢气出口与各干燥器的第二开口之间。
在本申请中，具体地，第一控制阀和第二控制阀的类型可以在一定的范围内选择，例如，可以是气动球阀。通过控制第一控制阀或第二控制阀的开关情况，能够实现各开口之间流路的切换，避免气流进入其他流路中，例如，通过开启脱氧模块出口与第一干燥器第一开口之间的第一控制阀，并关闭脱 氧模块出口与第二干燥器第一开口、第三干燥器第一开口之间的第一控制阀，能够开启脱氧模块与第一干燥器之间的流路，关闭脱氧模块与第二干燥器和第三干燥器之间的流路，使得脱氧后氢气进入第一干燥器中，而不会进入第二干燥器和第三干燥器中。
本申请中，再生循环模块还包括加热器5；
所述第二限气模块，具体用于供部分所述提纯氢气依次流经第一气气换热器4的所述第一气体通道、所述加热器5、所述第二干燥器2、所述第一气气换热器4的所述第二气体通道和所述第三干燥器3，形成再生通道，获得回收氢气。
在本申请中，氢气纯化系统中的三台干燥器共用一个再生循环模块，而再生循环模块包括加热器，因而本申请显著减少了加热器的数量，系统的制造成本较低；同时，再生循环系统中设置有第一气气换热器，使得再生前的低温再生氢气与再生后的高温再生尾气能够进行热量交换，这一方面能够充分利用高温再生尾气的余热，另一方面能够显著减少后续加热器和再生冷却器的功耗，因此，该系统的能耗较低。
根据本申请，第一干燥器1的第二开口、第二干燥器2的第二开口和第三干燥器3的第二开口还能够分别与加热器5的出口连通；第一气气换热器4的第一气体通道出口与加热器5的入口连通。其中，将提纯氢气分出一部分作为低温再生氢气从第一气气换热器的第一气体通道入口进入第一气气换热器的第一气体通道中进行换热处理，再经第一气气换热器的第一气体通道出口和加热器的入口进入加热器中进行加热处理，得到高温再生氢气。
根据本申请，所述第二控制阀还设置在所述加热器5的出口与各干燥器的第二开口之间。
根据本申请，加热器5上可以设有第六测温设备21，所述加热器5的出口处可以设有第七测温设备22。
根据本申请，所述再生循环模块还可以包括：冷却器8，用于对所述第二干燥器2进行降温；第三限气模块，用于供部分所述提纯氢气依次流经所述冷却器8、所述第二干燥器2、所述第一气气换热器4的第二气体通道和所述第三干燥器3，形成再生冷却通道。
其中，所述冷却器8的入口能够分别与所述第一干燥器1的第二开口、 所述第二干燥器2的第二开口和所述第三干燥器3的第二开口连通，所述冷却器8的出口能够分别与所述第一干燥器1的第二开口、所述第二干燥器2的第二开口和所述第三干燥器3的第二开口连通。
在本申请中，氢气纯化系统中的三台干燥器共用一个再生循环模块，而再生循环模块包括加热器和冷却器，因而本申请显著减少了加热器和冷却器的数量，系统的制造成本较低。
在本申请中，具体地，冷却器8的类型可以在一定的范围内选择，例如可以是吹冷冷却器，主要用于在干燥剂再生一段时间后，对来自用于待纯化氢气干燥的干燥器的部分提纯氢气进行降温处理，并使降温处理后的这部分提纯氢气进入用于干燥剂再生的干燥器中，以对再生后的高温再生干燥剂进行快速冷却，这一方面能够缩短再生过程的持续时间，另一方面能够使得再生干燥剂处于低温状态而增加其吸附能力。
也就是说，本申请系统中的待生干燥剂的再生过程至少包括两个操作，第一个操作是利用经第一气气换热器和加热器加热后的高温再生氢气带走待生干燥剂中水分，第二个操作是利用经冷却器冷却后的低温提纯氢气对第一个操作后得到的高温再生干燥剂进行快速冷却。
根据本申请，所述第三限气模块可以包括至少一个第三控制阀，第三控制阀可以设置在所述冷却器8的入口与各干燥器的第二开口之间，和/或，所述冷却器8的出口与各干燥器的第二开口之间。通过第三控制阀的调控，可以使得来自用于待纯化氢气干燥的干燥器的部分提纯氢气流向所述冷却器8，而不会流向第一气气换热器4的第一气体通道。
根据本申请，所述再生循环模块还可以包括再生冷却器6和第一汽水分离器7，所述再生冷却器6的入口与所述第一气气换热器4的第二气体通道出口连通，所述再生冷却器6的出口与所述第一汽水分离器7的入口连通，所述第一汽水分离器7的出口能够分别与所述第一干燥器1的第一开口、所述第二干燥器2的第一开口或所述第三干燥器3的第一开口连通。
根据本申请，所述脱氧模块还可以包括第二气气换热器10和脱氧器11，所述第二气气换热器10具有第一气体通道和第二气体通道，其中，所述第二气气换热器10的第一气体通道出口与所述脱氧器11的入口连通，所述脱氧器11的出口与所述第二气气换热器10的第二气体通道入口连通，所述第二气气换热器10的第二气体通道出口能够分别与所述第一干燥器1的第一开口、所述第二干燥器2的第一开口和所述第三干燥器3的第一开口连通。
在本申请中，具体地，由于第二气气换热器的设置，在脱氧器中完成脱氧后的氢气热气流能够回流到第二气气换热器的第二气体通道中，并对流经第一气体通道中的低温待纯化氢气进行热交换加热，从而使得待纯化氢气的温度升高，而脱氧后氢气的温度降低，这能够有效降低脱氧器和后续冷却冷凝器的功耗。
根据本申请，所述氢气纯化系统还可以包括冷却冷凝器12和第二汽水分离器13，其中，所述冷却冷凝器12的入口与所述第二气气换热器10的第二气体通道出口连通，所述冷却冷凝器12的出口与所述第二汽水分离器13的入口连通，所述第二汽水分离器13的出口能够分别与所述第一干燥器1的第一开口、所述第二干燥器2的第一开口和所述第三干燥器3的第一开口连通。
根据本申请，所述第一气气换热器4的第二气体通道入口与各干燥器的第一开口之间还可以设置有第一冷凝水排放管道14，所述第一冷凝水排放管道14的一端同时与所述第一气气换热器4的第二气体通道入口和各干燥器的第一开口连通；所述第二气气换热器10的第二气体通道入口与所述脱氧器11的出口之间还可以设置有第二冷凝水排放管道15，所述第二冷凝水排放管道15同时与所述第二气气换热器10的第二气体通道入口和所述脱氧器11的出口连通。第一冷凝水排放管道和第二冷凝水排放管道均用于排放气体流路中累积的冷凝水，避免冷凝水进入气气换热器中，影响换热效果。
根据本申请，所述第一冷凝水排放管道14和所述第二冷凝水排放管道15上均可以设有控制阀。
根据本申请，所述脱氧器11上可以设有第一测温设备16，所述脱氧器11的出口处可以设有第二测温设备17，所述第一干燥器1的第一开口处可以设有第三测温设备18，所述第二干燥器2的第一开口处可以设有第四测温设备19，所述第三干燥器3的第一开口处可以设有第五测温设备20。
根据本申请，所述第一干燥器1、所述第二干燥器2和所述第三干燥器3均为筒状结构，筒内设有分子筛干燥剂。由于本申请系统中的各干燥器均共用一个气气换热器和加热器，因此各干燥器中无需设置电加热设备，节能减排效果明显。
本申请的第二方面提供一种电解水制氢系统，所述电解水制氢系统可以包括电解水制氢模块和上述任意一项所述的氢气纯化系统，所述电解水制氢模块与所述氢气纯化系统的所述脱氧模块连通。
本申请的第三方面提供一种利用上述任意一项所述的系统来纯化氢气的方法，该方法可以包括操作S01～操作S07。
在操作S01中，使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气。其中，待纯化氢气例如可以是水电解氢气。
在操作S02中，使所述脱氧后氢气进入所述第一干燥器中进行干燥处理，得到所述提纯氢气。
在操作S03中，将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，得到高温再生氢气。
在操作S04中，停止向所述第二干燥器中通入所述脱氧后氢气，并使所述高温再生氢气进入所述第二干燥器中，对所述第二干燥器中的待生分子筛干燥剂进行吹干再生，得到高温再生尾气。
在操作S05中，使所述高温再生尾气进入所述第一气气换热器的所述第二气体通道中，与所述第一气体通道中的所述低温再生氢气进行换热处理，得到低温再生尾气。
在操作S06中，使所述低温再生尾气进入所述第三干燥器中进行干燥处理，得到回收氢气。
在操作S07中，使所述回收氢气与所述提纯氢气合并。
根据本申请，操作S04中，所述高温再生氢气与所述脱氧后氢气通入所述第二干燥器中的气体流向相反。
根据本申请，所述氢气纯化的方法还可以包括：重复操作S02～S07，在所述第二干燥器中对所述脱氧后氢气进行干燥处理，对所述第三干燥器中的待生分子筛干燥剂进行吹干再生，在所述第一干燥器中对所述低温再生尾气进行干燥处理；和/或，重复操作S02～S07，在所述第三干燥器中对所述脱氧后氢气进行干燥处理，对所述第一干燥器中的待生分子筛干燥剂进行吹干再生，在所述第二干燥器中对所述低温再生尾气进行干燥处理。
根据本申请，在操作S04中利用所述高温再生氢气对所述第二干燥器中的分子筛干燥剂进行吹干再生预设时长后，，所述氢气纯化的方法还可以包括操作S04-1和操作S04-2。
在操作S04-1中，停止使操作S03中的所述低温再生氢气进入所述第一气气换热器的第一气体通道中，以及，使一部分所述提纯氢气进入所述冷却器中进行冷却处理，得到吹冷氢气。
在操作S04-2中，停止使操作S04中的所述高温再生氢气进入所述第二 干燥器中，以及，使所述吹冷氢气进入所述第二干燥器中，对所述第二干燥器中的再生分子筛干燥剂进行吹冷处理，所产生气体替换操作S05中的所述高温再生尾气，继续执行操作S05～S07，其中，所述吹冷氢气的气体流向与所述高温再生氢气在所述第二干燥器中的气体流向相同。
根据本申请，操作S01中，所述使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气，可以包括：使所述待纯化氢气依次进入所述第二气气换热器的第一气体通道中进行换热处理，进入所述脱氧器中进行脱氧处理，进入所述第二气气换热器的第二气体通道中与所述第一气体通道中的所述待纯化氢气进行换热处理，得到所述脱氧后氢气。
根据本申请，操作S03中，从所述提纯氢气中分出的一部分的体积可以占所述提纯氢气总体积的10～15％。
根据本申请，操作S01中，所述脱氧处理的温度可以为85～100℃；操作S02中，所述干燥处理的温度可以为室温；操作S04中，所述吹干再生的温度可以为250～300℃；操作S06中，所述干燥处理的温度可以为室温。
根据本申请，操作S02中，在使所述脱氧后氢气进入所述第一干燥器中之前，所述纯化氢气的方法还包括：使所述脱氧后氢气依次进入所述冷却冷凝器中进行冷凝处理，进入所述第二汽水分离器中进行汽水分离处理。
根据本申请，操作S06中，在使所述低温再生尾气进入所述第三干燥器中进行干燥处理之前，所述纯化氢气的方法还包括：使所述低温再生尾气依次进入所述再生冷却器中进行冷凝处理，进入所述第一汽水分离器中进行汽水分离处理。
根据本申请，所述再生循环模块还包括加热器；
所述第二限气模块，具体用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述加热器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气；
操作S03具体包括：
将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，然后进入所述加热器中进行加热处理，得到所述高温再生氢气。
可选地，操作S03中，所述加热处理的温度为300～350℃。
需要说明的是，在本申请实施例中，方法部分的实施方式与系统部分的实施方式相同或类似，在此不再赘述。
下面通过实施例来进一步说明本申请，但是本申请并不因此而受到任何限制。本申请实施例中涉及的原料、试剂、仪器和设备，如无特殊说明，均可通过购买获得。
实施例1
基于图1所示的系统，采用如下方法进行水电解氢气的纯化：
(1)使待纯化氢气进入第二气气换热器的第一气体通道中进行换热处理，再进入脱氧器中进行脱氧处理，最后进入第二气气换热器的第二气体通道中与第一气体通道中的待纯化氢气进行换热处理，得到脱氧后氢气；
(2)使脱氧后氢气进入冷却冷凝器中进行冷凝处理，再进入第二汽水分离器中进行汽水分离处理，然后再从第一干燥器的第一开口进入第一干燥器中进行干燥处理，得到提纯氢气；
(3)将提纯氢气分出15％作为低温再生氢气进入第一气气换热器的第一气体通道中进行换热处理，然后进入加热器中进行加热处理，得到高温再生氢气；
(4)停止向第二干燥器的第一开口通入脱氧后氢气，并使高温再生氢气从第二干燥器的第二开口进入第二干燥器中，对第二干燥器中的待生分子筛干燥剂进行吹干再生，得到高温再生尾气；
(5)待步骤(4)中吹干再生结束后，停止使步骤(3)中的低温再生氢气进入第一气气换热器的第一气体通道中，以及，使一部分提纯氢气进入冷却器中进行冷却处理，得到吹冷氢气；停止使步骤(4)中的高温再生氢气进入第二干燥器中，以及，使吹冷氢气进入第二干燥器中，对第二干燥器中的再生分子筛干燥剂进行吹冷处理，得到吹冷后氢气，转入步骤(6)；
(6)使步骤(4)得到的高温再生尾气或步骤(5)得到的吹冷后氢气进入第一气气换热器的第二气体通道中与第一气气换热器的第一气体通道中的低温再生氢气进行换热处理，然后依次流经再生冷却器和第一汽水分离器，得到低温再生尾气；
(7)使低温再生尾气进入第三干燥器中进行干燥处理，得到回收氢气；
(8)待步骤(2)～(7)的操作持续24h后，将步骤(2)和(3)中与干燥器相关的操作转移至第二干燥器中，将步骤(4)～(6)中与干燥器 相关的操作转移至第三干燥器中，将步骤(7)中与干燥器相关的操作转移至第一干燥器中；
(9)24h后，将步骤(2)和(3)中与干燥器相关的操作转移至第三干燥器中，将步骤(4)～(6)中与干燥器相关的操作转移至第一干燥器中，将步骤(7)中与干燥器相关的操作转移至第二干燥器中；
(10)使所有的提纯氢气和所有的回收氢气合并，得到氢气产品，重复执行步骤(1)～(9)的操作，即可实现对水电解氢气的持续纯化。
以上结合附图详细描述了本申请的优选实施方式，但是，本申请并不限于上述实施方式中的具体细节，在本申请的技术构思范围内，可以对本申请的技术方案进行多种简单变型，这些简单变型均属于本申请的保护范围。
另外需要说明的是，在上述具体实施方式中所描述的各个具体技术特征，在不矛盾的情况下，可以通过任何合适的方式进行组合，为了避免不必要的重复，本申请对各种可能的组合方式不再另行说明。
此外，本申请的各种不同的实施方式之间也可以进行任意组合，只要其不违背本申请的思想，其同样应当视为本申请所公开的内容。

Claims (28)

  1. 一种氢气纯化系统，用于对待纯化氢气进行纯化形成提纯氢气，其中，所述氢气纯化系统包括：
    依次连通的脱氧模块、干燥模块和再生循环模块，所述干燥模块包括并联连接的第一干燥器、第二干燥器和第三干燥器；所述再生循环模块包括具有第一气体通道和第二气体通道的第一气气换热器；
    所述氢气纯化系统还包括：
    第一限气模块，用于供所述待纯化氢气依次流经所述脱氧模块和所述第一干燥器形成纯化通道，获得所述提纯氢气；
    第二限气模块，用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气。
  2. 根据权利要求1所述的氢气纯化系统，其中，所述第一干燥器、所述第二干燥器和所述第三干燥器均具有第一开口和第二开口，其中，所述第一干燥器的第一开口、所述第二干燥器的第一开口和所述第三干燥器的第一开口能够分别与所述脱氧模块的出口、所述第一气气换热器的第二气体通道入口和所述第一气气换热器的第二气体通道出口连通；所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口能够分别与提纯氢气出口、所述第一气气换热器的第一气体通道入口以及回收氢气出口连通；
    其中，所述提纯氢气出口用于输出所述提纯氢气，所述回收氢气出口用于输出所述回收氢气。
  3. 根据权利要求2所述的氢气纯化系统，其中，所述第一限气模块包括至少一个第一控制阀，所述第二限气模块包括至少一个第二控制阀；
    所述第一控制阀设置在所述脱氧模块的出口与各干燥器的第一开口之间以及所述提纯氢气出口与各干燥器的第二开口之间；
    所述第二控制阀设置在所述第一气气换热器的第一气体通道入口与各干燥器的第二开口之间、所述第一气气换热器的第二气体通道入口与各干燥器的第一开口之间、所述第一气气换热器的第二气体通道出口与各干燥器的 第一开口之间以及所述回收氢气出口与各干燥器的第二开口之间。
  4. 根据权利要求1所述的氢气纯化系统，其中，所述再生循环模块还包括：
    冷却器，用于对所述第二干燥器进行降温；
    第三限气模块，用于供部分所述提纯氢气依次流经所述冷却器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生冷却通道。
  5. 根据权利要求4所述的氢气纯化系统，其中，所述冷却器的入口能够分别与所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口连通，所述冷却器的出口能够分别与所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口连通。
  6. 根据权利要求5所述的氢气纯化系统，其中，所述第三限气模块包括至少一个第三控制阀，第三控制阀设置在所述冷却器的入口与各干燥器的第二开口之间，和/或，所述冷却器的出口与各干燥器的第二开口之间。
  7. 根据权利要求1所述的氢气纯化系统，其中，所述再生循环模块还包括再生冷却器和第一汽水分离器，所述再生冷却器的入口与所述第一气气换热器的第二气体通道出口连通，所述再生冷却器的出口与所述第一汽水分离器的入口连通，所述第一汽水分离器的出口能够分别与所述第一干燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
  8. 根据权利要求1所述的氢气纯化系统，其中，所述脱氧模块包括第二气气换热器和脱氧器，所述第二气气换热器具有第一气体通道和第二气体通道，其中，所述第二气气换热器的第一气体通道出口与所述脱氧器的入口连通，所述脱氧器的出口与所述第二气气换热器的第二气体通道入口连通，所述第二气气换热器的第二气体通道出口能够分别与所述第一干燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
  9. 根据权利要求8所述的氢气纯化系统，其中，所述氢气纯化系统还包括冷却冷凝器和第二汽水分离器，其中，所述冷却冷凝器的入口与所述第二气气换热器的第二气体通道出口连通，所述冷却冷凝器的出口与所述第二汽水分离器的入口连通，所述第二汽水分离器的出口能够分别与所述第一干 燥器的第一开口、所述第二干燥器的第一开口或所述第三干燥器的第一开口连通。
  10. 根据权利要求8所述的氢气纯化系统，其中，所述第一气气换热器的第二气体通道入口与各干燥器的第一开口之间还设置有第一冷凝水排放管道，所述第一冷凝水排放管道的一端同时与所述第一气气换热器的第二气体通道入口和各干燥器的第一开口连通；
    所述第二气气换热器的第二气体通道入口与所述脱氧器的出口之间还设置有第二冷凝水排放管道，所述第二冷凝水排放管道同时与所述第二气气换热器的第二气体通道入口和所述脱氧器的出口连通；
    所述第一冷凝水排放管道和所述第二冷凝水排放管道上均设有控制阀。
  11. 根据权利要求8所述的氢气纯化系统，其中，所述脱氧器上设有第一测温设备，所述脱氧器的出口处设有第二测温设备，所述第一干燥器的第一开口处设有第三测温设备，所述第二干燥器的第一开口处设有第四测温设备，所述第三干燥器的第一开口处设有第五测温设备。
  12. 根据权利要求3述的氢气纯化系统，其中，所述再生循环模块还包括加热器；
    所述第二限气模块，具体用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述加热器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气。
  13. 根据权利要求12所述的氢气纯化系统，其中，所述第一干燥器的第二开口、所述第二干燥器的第二开口和所述第三干燥器的第二开口还能够分别与所述加热器的出口连通；所述第一气气换热器的第一气体通道出口与所述加热器的入口连通。
  14. 根据权利要求12所述的氢气纯化系统，其中，所述第二控制阀还设置所述加热器的出口与各干燥器的第二开口之间。
  15. 根据权利要求12所述的氢气纯化系统，其中，所述加热器上设有第六测温设备，所述加热器的出口处设有第七测温设备。
  16. 根据权利要求1～15中任意一项所述的氢气纯化系统，其中，所述 第一干燥器、所述第二干燥器和所述第三干燥器均为筒状结构，筒内设有分子筛干燥剂。
  17. 一种电解水制氢系统，其中，所述电解水制氢系统包括电解水制氢模块和权利要求1～16中任意一项所述的氢气纯化系统，所述电解水制氢模块与所述氢气纯化系统的所述脱氧模块连通。
  18. 一种利用权利要求1所述的氢气纯化系统来纯化氢气的方法，其中，所述纯化氢气的方法包括：
    S01.使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气；
    S02.使所述脱氧后氢气进入所述第一干燥器中进行干燥处理，得到所述提纯氢气；
    S03.将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，得到高温再生氢气；
    S04.停止向所述第二干燥器中通入所述脱氧后氢气，并使所述高温再生氢气进入所述第二干燥器中，对所述第二干燥器中的待生分子筛干燥剂进行吹干再生，得到高温再生尾气；
    S05.使所述高温再生尾气进入所述第一气气换热器的所述第二气体通道中，与所述第一气体通道中的所述低温再生氢气进行换热处理，得到低温再生尾气；
    S06.使所述低温再生尾气进入所述第三干燥器中进行干燥处理，得到回收氢气；
    S07.使所述回收氢气与所述提纯氢气合并。
  19. 根据权利要求18所述的纯化氢气的方法，其中，操作S04中，所述高温再生氢气与所述脱氧后氢气通入所述第二干燥器中的气体流向相反。
  20. 根据权利要求19所述的纯化氢气的方法，其中，所述纯化氢气的方法还包括：重复操作S02～S07，在所述第二干燥器中对所述脱氧后氢气进行干燥处理，对所述第三干燥器中的待生分子筛干燥剂进行吹干再生，在所述第一干燥器中对所述低温再生尾气进行干燥处理；和/或，
    重复操作S02～S07，在所述第三干燥器中对所述脱氧后氢气进行干燥 处理，对所述第一干燥器中的待生分子筛干燥剂进行吹干再生，在所述第二干燥器中对所述低温再生尾气进行干燥处理。
  21. 根据权利要求18所述的纯化氢气的方法，其中，在操作S04中利用所述高温再生氢气对所述第二干燥器中的分子筛干燥剂进行吹干再生预设时长后，所述纯化氢气的方法还包括：
    S04-1.停止使操作S03中的所述低温再生氢气进入所述第一气气换热器的第一气体通道中，以及，使一部分所述提纯氢气进入所述冷却器中进行冷却处理，得到吹冷氢气；
    S04-2.停止使操作S04中的所述高温再生氢气进入所述第二干燥器中，以及，使所述吹冷氢气进入所述第二干燥器中，对所述第二干燥器中的再生分子筛干燥剂进行吹冷处理，所产生气体替换操作S05中的所述高温再生尾气，继续执行操作S05～S07，其中，所述吹冷氢气的气体流向与所述高温再生氢气在所述第二干燥器中的气体流向相同。
  22. 根据权利要求18所述的纯化氢气的方法，其中，操作S01中，使所述待纯化氢气进入所述脱氧模块中进行脱氧处理，得到脱氧后氢气，包括：
    使所述待纯化氢气依次进入所述第二气气换热器的第一气体通道中进行换热处理，进入所述脱氧器中进行脱氧处理，进入所述第二气气换热器的第二气体通道中与所述第一气体通道中的所述待纯化氢气进行换热处理，得到所述脱氧后氢气。
  23. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，操作S03中，从所述提纯氢气中分出的一部分的体积占所述提纯氢气总体积的10～15％。
  24. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，操作S01中，所述脱氧处理的温度为85～100℃；操作S02中，所述干燥处理的温度为室温；操作S04中，所述吹干再生的温度为250～300℃；操作S06中，所述干燥处理的温度为室温。
  25. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，操作S02中，在使所述脱氧后氢气进入所述第一干燥器中之前，所述纯化氢气的方法还包括：
    使所述脱氧后氢气依次进入所述冷却冷凝器中进行冷凝处理，进入所述第二汽水分离器中进行汽水分离处理。
  26. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，操作S06中，在使所述低温再生尾气进入所述第三干燥器中进行干燥处理之前，所述纯化氢气的方法还包括：
    使所述低温再生尾气依次进入所述再生冷却器中进行冷凝处理，进入所述第一汽水分离器中进行汽水分离处理。
  27. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，所述再生循环模块还包括加热器；
    所述第二限气模块，具体用于供部分所述提纯氢气依次流经所述第一气气换热器的所述第一气体通道、所述加热器、所述第二干燥器、所述第一气气换热器的所述第二气体通道和所述第三干燥器，形成再生通道，获得回收氢气；
    操作S03具体包括：
    将所述提纯氢气分出一部分作为低温再生氢气进入所述第一气气换热器的第一气体通道中进行换热处理，然后进入所述加热器中进行加热处理，得到所述高温再生氢气。
  28. 根据权利要求18～22中任意一项所述的纯化氢气的方法，其中，操作S03中，所述加热处理的温度为300～350℃。
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