Electrochemical hydrogen membrane separator

Abstract

The application provides an electrochemical hydrogen membrane separator, comprising a fuel cell assembly and a wire, wherein the anode and the cathode of the fuel cell assembly are short-circuited by the wire; the fuel cell assembly comprises an anode current collector, an anode pole plate, an anode gasket, an anode gas diffusion layer, a membrane electrode, a cathode gas diffusion layer, a cathode gasket, a cathode pole plate and a cathode current collector, and the application mainly utilizes the wire connected at the anode and the cathode of the fuel cell to form an external short circuit, changes the thermodynamic reversible potential by increasing the gas pressure difference between the anode and the cathode or increasing the operation temperature, and then generates a voltage driving force, so as to achieve the effect of completing the spontaneous separation of hydrogen from the anode to the cathode without an external power supply.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of hydrogen separation, in particular, especially relates to an electrochemical hydrogen membrane separator. BACKGROUND

[0002] With the increasing importance of hydrogen energy industry in the energy structure of our country, hydrogen separation and purification has been widely concerned by the scientific and industrial circles. Membrane separation technology is one of the current research hotspots in the field of science and technology because of its low energy consumption, simple equipment, small occupation area and other advantages. The traditional membrane separation technology takes pressure difference as the driving force, and the gas molecules mainly pass through the pores of the porous membrane in the way of dissolution-diffusion. The bottleneck of this technology is that the permeability and selectivity of the gas cannot be considered at the same time, it is difficult to break through the traditional membrane separation Robeson upper limit, and the separation of hydrogen-poor gas requires high pressure difference, which is easy to crush the separation membrane.

[0003] The electrochemical method for separating hydrogen has the advantages of high selectivity, high efficiency (especially for hydrogen-poor mixed gas), high hydrogen purity and other advantages, and is a new type of hydrogen membrane separation technology with development potential. According to the patent 201911384959.9, the existing electrochemical hydrogen separation technology (commonly known as electrochemical hydrogen pump) is to promote the hydrogen oxidation reaction at the anode and the hydrogen reduction reaction at the cathode by applying an external voltage / current, thereby completing the separation of hydrogen and mixed gas. The main challenge of the electrochemical hydrogen pump technology is that an external voltage is needed to drive the reaction, and the larger the system is, the higher the energy consumption is. SUMMARY

[0004] According to the above-mentioned technical problems of traditional electrochemical hydrogen pump needing to provide additional voltage and high energy consumption after module assembly engineering amplification, an electrochemical hydrogen membrane separator is provided. By connecting the anode and cathode of the fuel cell with a wire to short-circuit the outside, and by increasing the working temperature or changing the gas pressure difference between the anode and cathode to form a thermodynamic voltage driving force, the spontaneous separation process of hydrogen from the anode to the cathode is completed without external power supply. The present application provides new technical reserves for hydrogen separation and purification, and accelerates the development of electrochemical hydrogen membrane separation. The technical means adopted by the present application is as follows:

[0005] An electrochemical hydrogen membrane separator, characterized in that it comprises: a fuel cell assembly and a wire, the anode and cathode of the fuel cell assembly are short-circuited by the wire; the fuel cell assembly comprises an anode current collector, an anode plate, an anode gasket, an anode gas diffusion layer, a membrane electrode, a cathode gas diffusion layer, a cathode gasket, a cathode plate and a cathode current collector, and the anode current collector, the anode plate, the anode gasket, the anode gas diffusion layer, the membrane electrode, the cathode gas diffusion layer, the cathode gasket, the cathode plate and the cathode current collector are arranged in the fuel cell in sequence.

[0006] Further, the wire is made of silver wire, copper wire, iron wire and their mixture.

[0007] Further, the membrane electrode comprises a gas diffusion layer, a catalytic layer and a proton exchange membrane, the catalytic layer comprises a catalyst and an electrode binder; the proportion of the binder in the catalytic layer is 5-60wt%.

[0008] Further, the gas diffusion layer is made of at least one of carbon paper, carbon felt, nickel mesh, nickel felt, titanium mesh and titanium felt.

[0009] Further, the catalyst can be at least one of Pt black, Pt / C, Pt alloy and Pt alloy / C.

[0010] The electrode binder can be at least one of polytetrafluoroethylene (PTFE), perfluorosulfonic acid resin, polybenzimidazole, polyaryl piperidine, sulfonated polyaryl polymer or phosphonated polyaryl polymer.

[0011] Further, the proportion of the binder in the catalytic layer is 5-35wt%.

[0012] Further, the proton exchange membrane can be at least one of perfluorosulfonic acid proton exchange membrane, phosphoric acid doped polybenzimidazole proton exchange membrane, phosphoric acid doped polyaryl piperidine proton exchange membrane, sulfonated polyether ether ketone proton exchange membrane, sulfonated polysulfone proton exchange membrane, sulfonated polystyrene proton exchange membrane, phosphonated polystyrene proton exchange membrane and phosphonated polyperfluorobiphenyl proton exchange membrane.

[0013] The application further provides a method for electrochemically separating hydrogen, which is characterized by comprising the following steps:

[0014] (1) preparing a fuel cell assembly;

[0015] (2) connecting the anode and the cathode of the fuel cell through a wire;

[0016] (3) introducing the mixed gas to be separated into the anode end of the fuel cell and introducing purge gas into the cathode end of the fuel cell, setting the temperature of the fuel cell and adjusting the back pressure of the anode side of the fuel cell.

[0017] Further, the temperature is 100-160℃ and the purge gas is nitrogen.

[0018] Further, the back pressure is 0-0.15Mpa.

[0019] Compared with the prior art, the application has the following advantages:

[0020] 1. The electrochemical hydrogen membrane separator provided by the application is a self-driven separator, compared with the existing electrochemical hydrogen separation technology which needs an external power supply, the application forms an external short circuit by connecting the anode and the cathode of the fuel cell with a wire, so that the hydrogen is spontaneously separated from the anode to the cathode through an electrochemical reaction without an external power supply, realizing the self-driving of the separated hydrogen, compared with the traditional electrochemical hydrogen pump technology, the technology greatly reduces the energy consumption, and the equipment is simple and occupies a small area.

[0021] 2. The electrochemical hydrogen membrane separator provided by the application separates hydrogen through wire short-circuiting, hydrogen oxidation reaction occurs in the anode to generate hydrogen protons and electrons, the protons are conducted to the cathode through the internal proton exchange membrane, and the electrons are conducted to the cathode through the external wire, and the protons and the electrons combine to generate hydrogen gas through hydrogen reduction reaction at the cathode. Other gases hardly pass through the dense proton exchange membrane, so the technology has high selectivity for separating hydrogen.

[0022] 3. The electrochemical hydrogen membrane separator provided by the application can improve the thermodynamic voltage and thus improve the hydrogen separation driving force by increasing the operating temperature or the gas pressure difference between the anode and the cathode within a certain range, so that the hydrogen permeation rate of the technology is controllable.

[0023] 4. In the electrochemical hydrogen membrane separator provided by the application, when the binder accounts for 5% to 35% in the catalyst layer, the permeation rate and selectivity of the separated hydrogen are relatively good, and when the PTFE accounts for 15wt%, the permeation rate and selectivity of the separated hydrogen are the highest. Because the electrode binder can optimize the structure of the catalyst layer, the catalyst layer becomes more stable. When the PTFE content is too small, the binding and uniform dispersion of the electrode are weakened, but when the PTFE content is too much, the catalyst layer becomes thicker and heavier, which blocks the active sites of the catalyst, increases the mass transfer resistance, and makes the hydrogen separation effect worse.

[0024] 5. In the electrochemical hydrogen membrane separator provided by the application, the sweep gas is introduced into the cathode of the fuel cell assembly, which can provide the driving force for transporting hydrogen, so that the generated hydrogen is more quickly conducted to the cathode, and the reaction proceeds in the forward direction.

[0025] Based on the above reasons, the application can be widely popularized in the field of hydrogen separation technology. BRIEF DESCRIPTION OF DRAWINGS

[0026] In order to more clearly illustrate the technical solutions in the embodiments of the application or the prior art, the drawings needed in the following embodiment or prior art description will be briefly introduced. Obviously, the drawings in the following description are some embodiments of the application, and other drawings can also be obtained by those skilled in the art without creative labor.

[0027] Figure 1 A schematic diagram of an electrochemical hydrogen membrane separator of the present application.

[0028] Figure 2 A schematic diagram of a fuel cell assembly of the electrochemical hydrogen membrane separator of the present application.

[0029] Figure 3 A schematic diagram of a test platform of the electrochemical hydrogen membrane separator of the present application.

[0030] Figure 4 A chart of the gas permeability and selectivity of the electrochemical hydrogen separator of the present application for separating hydrogen gas with or without wires at the anode and cathode.

[0031] Figure 5 A chart of the permeability and selectivity of the electrochemical hydrogen separator of the present application for separating hydrogen gas at different PTFE ratios.

[0032] Figure 6 A chart of the gas permeability and selectivity of the electrochemical hydrogen membrane separator of the present application for separating hydrogen gas at different temperatures.

[0033] Figure 7 A chart of the gas permeability and selectivity of the electrochemical hydrogen membrane separator of the present application for separating hydrogen gas at different anode back pressures.

[0034] In the figure: 1, membrane electrode; 2, anode gas diffusion layer; 3, cathode gas diffusion layer; 4, anode gasket; 5, cathode gasket; 6, anode plate; 7, cathode plate; 8, anode current collector plate; 9, cathode current collector plate; 10, rotor flow meter; 11, mass flow meter; 12, temperature controller; 13, fuel cell assembly; 14, electrochemical workstation; 15, wire; 16, ball valve; 17, ball valve; 18, pressure gauge; 19, pressure control valve; 20, diaphragm flow meter; 21, gas chromatograph. DETAILED DESCRIPTION

[0035] It should be noted that the embodiments in the present application and the features in the embodiments can be combined with each other without conflict. The present application will be described in detail below with reference to the accompanying drawings and in conjunction with the embodiments.

[0036] In order to make the objects, technical solutions and advantages of the embodiments of the present application clearer, the following will clearly and completely describe the technical solutions in the embodiments of the present application with reference to the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments of the present application. The following description of at least one example embodiment is merely illustrative in nature and is in no way limiting on the application or its applications or uses. Based upon a review of the embodiments contained herein, all other embodiments that are apparent to those of ordinary skill in the art, and to practitioners thereof, in which equal or substantially equivalent results are achieved, belong within the scope of the present application.

[0037] It should be noted that the terminology used herein is for the purpose of describing specific embodiments only and is not intended to be limiting of example embodiments in accordance with the present application. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise. It will be further understood that the terms "comprises" and / or "comprising," when used in this specification, specify the presence of stated features, steps, operations, elements, components, and / or groups thereof, but do not preclude the presence or addition of one or more other features, steps, operations, elements, components, and / or groups thereof.

[0038] The relative arrangement of parts and steps, numerical expressions, and numerical values set forth in the examples are not intended to limit the scope of the application unless otherwise specifically stated. It should be apparent that the dimensions of the various parts shown in the drawings are not to scale and are only meant to illustrate the general principles of the application. Techniques, methods, and apparatus known to those of ordinary skill are not discussed in detail because they would be apparent in light of the teachings herein. All examples shown and discussed herein are intended to be illustrative of the application and not limiting thereof. Thus, other examples of the example embodiments can have different values. It should be noted that like reference numerals and letters in the various figures indicate like elements, and therefore, further discussion of the same will not be repeated in the subsequent figures.

[0039] In the description of the present application, it should be understood that the orientation words such as "front, back, up, down, left, right", "transverse, vertical, perpendicular, horizontal" and "top, bottom" and the like indicated orientation or position relationship are generally based on the orientation or position relationship shown in the drawings, and are only for the convenience of describing the present application and simplifying the description, and in the absence of contrary description, these orientation words do not indicate and imply that the indicated device or element must have a particular orientation or be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the scope of protection of the present application: the orientation words "inner, outer" refer to the inner and outer relative to the contour of each component.

[0040] For purposes of the description hereinafter, spatial

[0041] In addition, it should be noted that the terms "first", "second", and so on can be used herein to describe various elements, however, the elements should not be limited by these terms. The terms are only used to distinguish one element from another. Thus, the "first" element discussed above could be termed a "second" element without departing from the teachings of the present application. The above terms can be used interchangeably when appropriate. Unless explicitly stated otherwise, elements described herein can also be used in combination or configured in various combinations other than the ones specifically described herein.

[0042] As Figures 1-7As shown, the present application provides an electrochemical hydrogen separator, comprising: a fuel cell assembly 13 and a wire 15, the anode and cathode of the fuel cell assembly 13 are short-circuited through the wire 15; the fuel cell assembly 13 comprises an anode current collector plate 8, an anode polar plate 6, an anode PTFE gasket 4, an anode gas diffusion layer 2, a membrane electrode 1, a cathode gas diffusion layer 3, a cathode PTFE gasket 5, a cathode polar plate 7 and a cathode current collector plate 9; the wire 15 can be made of silver wire, copper wire, iron wire and mixed wire and other high-conductivity materials; the membrane electrode 1 comprises a gas diffusion layer, a catalyst layer and a proton exchange membrane, and the preparation method can use spraying or scraping coating method; the gas diffusion layer can be made of at least one of carbon paper, carbon felt, nickel mesh, nickel felt, titanium mesh, titanium felt or other porous conductive materials; the catalyst layer comprises a catalyst and an electrode binder; the catalyst can be at least one of Pt black, Pt / C, Pt alloy or Pt alloy / C; the electrode binder can use at least one of polytetrafluoroethylene, perfluorosulfonic acid resin, polybenzimidazole, polyaryl piperidine, sulfonated polyaryl polymer or phosphated polyaryl polymer; the proton exchange membrane can be at least one of perfluorosulfonic acid proton exchange membrane, phosphoric acid doped polybenzimidazole proton exchange membrane, phosphoric acid doped polyaryl piperidine proton exchange membrane, sulfonated polyether ether ketone proton exchange membrane, sulfonated polysulfone proton exchange membrane, sulfonated polystyrene proton exchange membrane, phosphated polystyrene proton exchange membrane and phosphated polyperfluorobiphenyl proton exchange membrane; the scraping coating method is to coat the catalyst and the electrode binder directly on the gas diffusion layer to obtain a gas diffusion electrode, and then press the proton exchange membrane and two pieces of the gas diffusion electrode together to obtain the membrane electrode 1; the spraying method is to spray the catalyst and the electrode binder directly on the gas diffusion layer to obtain a gas diffusion electrode, and then press the proton exchange membrane and two pieces of the gas diffusion electrode together to obtain the membrane electrode 1.

[0043] Embodiment 1

[0044] The present application provides a preparation method of the above-mentioned membrane electrode 1 (MEA), comprising the following steps:

[0045] Step 1: dilute the electrode binder (polytetrafluoroethylene, perfluorosulfonic acid resin, polybenzimidazole, polyaryl piperidine, sulfonated polyaryl polymer or phosphated polyaryl polymer) solution with ethanol, then add a certain amount of catalyst (Pt black, Pt / C, Pt alloy or Pt alloy / C) to it, and ultrasonic dispersion at 0℃ for at least 2 hours, so that the electrode binder and the catalyst are fully dispersed in ethanol to obtain a catalyst slurry.

[0046] Step 2: Preparation of electrodes by scraping method: after ultrasonic dispersion, a certain amount of catalyst ink (according to the specific electrode area) is taken with a pipette and evenly dropped on one side of the carbon paper, then it is gently and evenly scraped on the whole carbon paper with a scraper, and after the solvent is volatilized, it is gently and evenly scraped again. Preparation of electrodes by spraying method: after ultrasonic dispersion, the catalyst is evenly sprayed on the whole carbon paper with a spray gun.

[0047] Step 3: The electrodes prepared in the above steps are placed in a tube furnace or a nitrogen-filled oven for drying to further volatilize the solvent.

[0048] Step 4: The proton exchange membrane used is at least one of perfluorosulfonic acid proton exchange membrane, phosphoric acid doped polybenzimidazole proton exchange membrane, phosphoric acid doped polyaryl piperidine proton exchange membrane, sulfonated polyether ether ketone proton exchange membrane, sulfonated polysulfone proton exchange membrane, sulfonated polystyrene proton exchange membrane, phosphonated polystyrene proton exchange membrane, phosphonated polyperfluorobiphenyl proton exchange membrane

[0049] Step 5: Finally, the high-temperature proton exchange membrane prepared above and two electrodes are pressed together to obtain a membrane electrode 1.

[0050] The membrane electrode prepared above is assembled with a gas diffusion layer, a sealing gasket, a cathode and anode two polar plates, a cathode and anode two current collector plates, and a wire connected between the two current collector plates to obtain a self-driven electrochemical hydrogen membrane separator, as shown in Figure 2 .

[0051] Example 2

[0052] The present application relates to an electrochemical hydrogen separator, mainly composed of a fuel cell assembly 13 and a wire 15.

[0053] The fuel cell assembly 15 includes an anode current collector plate 8, an anode polar plate 6, an anode PTFE gasket 4, an anode gas diffusion layer 2, a membrane electrode 1, a cathode gas diffusion layer 3, a cathode PTFE gasket 5, a cathode polar plate 7, a cathode current collector plate 9, and the assembly is as shown in Figure 2 .

[0054] The test platform of the hydrogen separator is shown in the accompanying Figure 3 , and the specific operation mode is as follows:

[0055] Step 1: Turn on the hydrogen alarm and check the air tightness of the device;

[0056] Step 2: Nitrogen is introduced into the anode and cathode respectively, and the readings of the soap film flowmeter 20 and the rotor flowmeter 10 are consistent, indicating good air tightness;

[0057] Step 3: Nitrogen and hydrogen-containing mixed gas are introduced into the cathode and anode respectively, and the flow rate is set.

[0058] Step 4: Turn on the temperature controller 12 for heating the mixed gas pipeline and the electrode plate respectively to the set temperature.

[0059] Step 5: After the temperature is stable, adjust the gas flow to the predetermined value, and control the anode side pressure to a certain value.

[0060] Step 6: Close the gas chromatograph 21 valve, measure the flow rate at the cathode outlet, then close the ball valve 16 valve and open the ball valve 17 valve, and record the gas chromatograph data.

[0061] When closing, turn off the heating power supply, pressure control valve, gas inlet, gas chromatograph in sequence, and cool the temperature to room temperature before disassembling the battery.

[0062] Example 3

[0063] Prepare the electrode with carbon paper, Pt / C catalyst, and PTFE electrode binder according to the following steps:

[0064] Step 1: Weigh the Pt / C catalyst with a target loading of 0.4 mg Pt / cm2, and disperse it in an ethanol solvent;

[0065] Step 2: Add polytetrafluoroethylene (PTFE) binder to prepare a catalyst slurry, and the weight percentage of PTFE in the electrode catalyst layer is 15%;

[0066] Step 3: Ultrasonically disperse the catalyst slurry at 0°C for at least 2 hours, and then uniformly scrape the slurry on the carbon paper.

[0067] Assemble the above prepared membrane electrode 1 with the gas diffusion layer, gasket, anode and cathode plates, and anode and cathode current collectors to form a fuel cell.

[0068] Pass the mixed gas with H2 and CO2 ratio of 1:1 at the anode end of the fuel cell, and pass the purge gas nitrogen at the cathode end of the fuel cell, with both temperatures set to 120°C, the anode mixed gas flow rate is 100 mL / min, and the operation is under normal pressure. Test the hydrogen permeation rate J t and selectivity S. Wherein the gas permeation rate and selectivity are calculated according to the following formulas (1) and (2) respectively:

[0069]

[0070]

[0071] Where Q is the volume flow rate of the permeation side gas under standard conditions (mL / min); y ip is the concentration of gas i on the permeation side; y if is the concentration of gas i on the raw material side (0.5); P f is the pressure of the raw material side gas (cmHg); P pP is the permeation side pressure (cmHg); A is the effective membrane area (m 2 ), T is the working temperature (K), and T0=273.15 K.

[0072] The results show that the gas permeation rate of separated hydrogen is greatly improved after connecting the wires, and the gas permeation rate of separated hydrogen is low without the wires, but the selectivity of separated hydrogen is high. Figure 4

[0073] Because without the wires, a closed loop cannot be formed, and electrons cannot reach the cathode from the anode, resulting in less permeation of separated hydrogen, the hydrogen permeation rate is low. At the same time, no potential difference can be formed between the cathode and the anode, and there is no driving force, resulting in less permeation flux of impurity gas, so the selectivity of separated hydrogen is high without the wires.

[0074] Example 4

[0075] The weight percentage of PTFE in the electrode catalyst layer was changed to 5%, and the other processes were the same as in Example 3. The hydrogen permeation rate and selectivity were tested, and the test results are shown in Table 2. Figure 5

[0076] Example 5

[0077] The weight percentage of PTFE in the electrode catalyst layer was changed to 25%, and the other processes were the same as in Example 3. The hydrogen permeation rate and selectivity were tested, and the test results are shown in Table 2. Figure 5

[0078] Example 6

[0079] The weight percentage of PTFE in the electrode catalyst layer was changed to 45%, and the other processes were the same as in Example 3. The hydrogen permeation rate and selectivity were tested, and the test results are shown in Table 2. Figure 5

[0080] Example 7

[0081] The weight percentage of PTFE in the electrode catalyst layer was changed to 60%, and the other processes were the same as in Example 3. The hydrogen permeation rate and selectivity were tested, and the test results are shown in Table 2. Figure 5

[0082] The hydrogen permeation rate and selectivity of separated hydrogen under different PTFE ratios in Example 3-Example 7 are shown in Table 2. Figure 5 As can be seen from Table 2, when the PTFE content is 5-60wt% in the present application, excellent hydrogen separation performance is exhibited, and when the PTFE ratio is 5%-35%, the permeation rate and selectivity of separated hydrogen are relatively good. Figure 5

[0083] ​​​​​​Example 8

[0084] The self-driven hydrogen membrane separator was assembled by using the electrode catalyst layer with 15% PTFE weight percentage, the mixed gas with H2 and CO2 ratio of 1:1 was passed through the anode end of the fuel cell, the sweeping gas nitrogen was passed through the cathode end of the fuel cell, the operating temperature was changed (100-160℃) at normal pressure, and other processes were the same as in Example 3. The hydrogen permeation rate and selectivity at different temperatures were tested as shown in Figure 6

[0085] Example 9

[0086] The self-driven hydrogen membrane separator was assembled by using the electrode with 15% PTFE weight percentage, the mixed gas with H2 and CO2 ratio of 1:1 was passed through the anode end of the fuel cell, the sweeping gas nitrogen was passed through the cathode end of the fuel cell, the back pressure was added on the anode side (0-0.15 MPa), and other processes were the same as in Example 3. The hydrogen permeation rate and selectivity at different back pressures were tested as shown in Figure 7

[0087] From Figure 6 and Figure 7 It can be seen that, within the temperature and pressure range provided in the present application, excellent hydrogen permeation rate and selectivity are exhibited. With the increase of temperature and pressure, the gas permeation rate for separating hydrogen gradually increases, and the selectivity for separating hydrogen decreases, but still remains at an excellent and effective level. This is because the temperature and / or the voltage driving force increases, the permeation flux of hydrogen increases, and the permeation flux of impurity gas also increases, so the selectivity for separating hydrogen decreases after the temperature and / or pressure increases. The technical solution provided in the present application can adjust the temperature and / or pressure according to actual needs to select the advantages of permeation rate and selectivity, which is simple and fast.

[0088] Finally, it should be noted that: the above examples are only used to illustrate the technical solutions of the present application, and not to limit them; although the present application has been described in detail with reference to the foregoing examples, those skilled in the art should understand that: it can still modify the technical solutions recorded in the foregoing examples, or make equivalent replacement for part or all of the technical features; and these modifications or replacements do not make the essence of the corresponding technical solution deviate from the scope of the technical solutions of the embodiments of the present application.​​

Claims

1. A method of electrochemically separating hydrogen gas, characterized by, The application relates to a fuel cell assembly and a wire, the anode and the cathode of the fuel cell assembly are short-circuited through the wire; the fuel cell assembly comprises an anode current collector, an anode plate, an anode gasket, an anode gas diffusion layer, a membrane electrode, a cathode gas diffusion layer, a cathode gasket, a cathode plate and a cathode current collector, which are arranged in the fuel cell in sequence. The application specifically comprises the following steps: (1) preparing a fuel cell assembly; (2) connecting the anode and the cathode of the fuel cell through a wire; (3) feeding a mixed gas to be separated into the anode end of the fuel cell, feeding a purge gas into the cathode end of the fuel cell, setting the temperature of the fuel cell, and adjusting the back pressure of the anode side of the fuel cell.

2. The method of electrochemically separating hydrogen gas of claim 1, wherein, The wire is made of silver wire, copper wire, iron wire or a mixture thereof.

3. The method of claim 1, wherein, The membrane electrode comprises a gas diffusion layer, a catalyst layer and a proton exchange membrane, the catalyst layer comprises a catalyst and an electrode binder; the proportion of the binder in the catalyst layer is 5-60wt%.

4. The method of claim 3, wherein, The gas diffusion layer is made of at least one of carbon paper, carbon felt, nickel mesh, nickel felt, titanium mesh or titanium felt.

5. The method of claim 4, wherein, The catalyst can be at least one of Pt black, Pt / C, Pt alloy or Pt alloy / C; The electrode binder can be at least one of polytetrafluoroethylene, perfluorosulfonic acid resin, polybenzimidazole, polyaryl piperidine, sulfonated polyaryl polymer or phosphonated polyaryl polymer.

6. The method of claim 3, wherein, The proportion of the binder in the catalyst layer is 5-35wt%.

7. The method of claim 3, wherein, The proton exchange membrane can be at least one of perfluorosulfonic acid proton exchange membrane, phosphoric acid-doped polybenzimidazole proton exchange membrane, phosphoric acid-doped polyaryl piperidine proton exchange membrane, sulfonated polyether ether ketone proton exchange membrane, sulfonated polysulfone proton exchange membrane, sulfonated polystyrene proton exchange membrane, phosphonated polystyrene proton exchange membrane and phosphonated polyperfluorobiphenyl proton exchange membrane.

8. The method of claim 1, wherein, The temperature is 100-160 o C; the purge gas is nitrogen.

9. The method of claim 1, wherein, The back pressure is 0-0.15Mpa.

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