TWI471262B - Filtration-enhanced hydrogen generator - Google Patents

Description

Separation aid hydrogen generator

This invention relates to a hydrogen generator, and more particularly to a separation assisted hydrogen generator.

Hydrogen energy is an energy type that humans may use in the future. Its use is mainly combined with fuel cell power generation or direct combustion. The reorganization of fossil raw materials is currently the main hydrogen production technology, and it is difficult to achieve the short-term ideal for large-scale hydrogen production from renewable energy. Therefore, reorganization is the main hydrogen production technology in the next 20-30 years.

Membrane separation and recombination is one of the most popular hydrogen production technologies in recent years. It uses a hydrogen separation membrane to remove hydrogen from the reaction process, destroying the chemical equilibrium and increasing the conversion rate of the reactants, while obtaining high-purity hydrogen for fuel. Battery performance is played.

However, the most common hydrogen separation membranes currently operate at temperatures ranging from 300 to 400 degrees Celsius. For recombination reactions with lower reaction temperatures, such as methanol recombination, they cannot be used directly, otherwise hydrogen embrittlement will occur. .

The present invention provides a separation assisted hydrogen generator that allows the recombination reaction and the membrane separation mechanism to be each within the most appropriate operating temperature range to maintain the performance of the recombination reaction and the life of the hydrogen hydride membrane.

The invention provides a separation assisting hydrogen generator, which can adjust the temperature of the feed to the proper operating temperature range of the mechanism before entering the recombination reaction and the membrane separation mechanism to maintain the performance of the recombination reaction and the life of the hydrogen absorbing membrane. .

The invention provides a separation assisting hydrogen generator, which can effectively improve the conversion rate, increase the hydrogen production rate, and make the purity of the produced hydrogen high.

The embodiment of the invention provides a separation assisted hydrogen generator, comprising a first recombination section, a first hydrogen filtration membrane section, a second recombination section, a second hydrogen filtration membrane section, a first heat exchanger and a second heat exchanger. The first recombination section is used to recombine the feed to form a first recombination atmosphere. The first hydrogen permeate membrane section is used to filter the first recombination atmosphere to form a first product and a first residual gas. The second recombination section is used to recombine the first residual gas to form a second recombination atmosphere. The second hydrogen permeate membrane section is used to filter the second recombination atmosphere to form a second product and a second residual gas. The first heat exchanger is coupled to the first recombination section and the first hydrogen permeate membrane section for heating the feed and receiving the first recombination atmosphere, which is heated before the first recombination gas stream enters the first hydrogen permeation membrane section. The second heat exchanger is coupled to the second recombination section and the second hydrogen permeate membrane section for receiving the second recombination atmosphere and heating the second recombination atmosphere before flowing into the second hydrogen permeate membrane section.

The embodiment of the invention provides a separation assisted hydrogen generator, comprising a first recombination section, a first hydrogen filtration membrane section, a second recombination section, a second hydrogen filtration membrane section and a heat exchange device. The first recombination section is used to recombine the feed to form a first recombination atmosphere. The first hydrogen permeate membrane section is used to filter the first recombination atmosphere to form a first product and a first residual gas. The second recombination section is used to recombine the first residual gas to form a second recombination atmosphere. The second hydrogen permeate membrane section is used to filter the second recombination atmosphere to form a second product and a second residual gas. The third heat exchanger is connected to the first hydrogen permeable membrane section and the second recombination section for receiving the first residual gas, so that the first residual gas enters the second recombination section, and the fuel or air that enters a combustion chamber Or a mixture of the two is heat exchanged, and the fourth heat exchanger is connected to the second hydrogen permeable membrane section for receiving the second residual gas, the second residual gas and the fuel or air flowing into the combustion chamber or both The mixture of the people undergoes heat exchange.

Based on the above, the separation assisted hydrogen generator of the embodiment of the present invention allows the recombination reaction and the membrane separation mechanism to be each within the most appropriate operating temperature range to maintain the performance of the recombination reaction and the life of the hydrogen hydride membrane.

The separation assisting hydrogen generator of the embodiment of the invention can adjust the temperature of the feed to the proper operating temperature range of the mechanism before entering the recombination reaction and the membrane separation mechanism to maintain the performance of the recombination reaction and the hydrogen absorbing membrane. life.

The separation assisting hydrogen generator of the embodiment of the invention can effectively increase the conversion rate, increase the hydrogen production rate, and make the purity of the produced hydrogen high.

The above described features and advantages of the present invention will be more apparent from the following description.

FIG. 1 is a schematic diagram of a separation assisted hydrogen generator according to an embodiment of the invention.

Referring to FIG. 1, the membrane type hydrocarbon recombination hydrogen generator 10 includes a combustion chamber 12, a heat exchanger unit 16, a recombination group 18 and a hydrogen permeation membrane group 20. The heat exchanger device 16 of the present embodiment includes a first heat exchanger 16a, a second heat exchanger 16b, a third heat exchanger 16c and a fourth heat exchanger 16d; the recombination group 18 includes a first recombination section 18a and a The second recombination section 18b; the hydrogen permeation membrane section group 20 includes the first hydrogen permeation membrane section 20a and the second hydrogen filtration membrane section 20b, however, the present invention is not limited thereto. In the embodiment of the present invention, the first recombination section 18a and the first hydrogen absorbing membrane section 20a are separated from each other and communicated by the flow channel 52. The first hydrogen absorbing membrane 20a and the second recombination section 18b are separated from each other and communicated by the flow path 54. The second recombination section 18b and the second hydrogen absorbing membrane 20b are separated from each other and communicated by the flow path 56.

The recombination feed which can be used in the separation assisted hydrogen generator 10 of the present invention is a method in which the reformed gas formed after the recombination reaction has a lower temperature, for example, a film lower than the hydrogen filtration membrane segment (for example, palladium or The palladium alloy can withstand the temperature limit (for example, below 300 degrees Celsius), and it is easy to cause hydrogen embrittlement of the film. The feed is for example a mixture comprising hydrocarbons and water. Hydrocarbons include fossil raw materials or renewable energy sources. The fossil raw materials are, for example, methanol, ethanol, and dimethyl ether; and the renewable energy source is, for example, alcohol produced by fermentation of biomass. In one embodiment, the fuel used to generate heat is, for example, methanol, ethanol or dimethyl ether. In one embodiment, the feed may pass through the sixth heat exchanger 16f and the fifth heat exchanger 16e in the heat recovery zone for heat exchange before entering the first heat exchanger 16a. The feed is heated by the hot fluid of the first heat exchanger 16a to a temperature range suitable for the recombination reaction, for example, from 150 to 350 degrees Celsius. The hot fluid of the first heat exchanger 16a is, for example, a flue gas generated after combustion of the fuel and air. The combustion gas passing through the first heat exchanger 16a first flows through the sixth heat exchanger 16f to carry out the heat exchange before leaving the reformer.

The first recombination section 18a is used to recombine the feed. More specifically, the first recombination section 18a is recombined through the feed of the sixth heat exchanger 16f, the fifth heat exchanger 16e, and the first heat exchanger 16a to form a first recombination atmosphere containing hydrogen. In an exemplary embodiment, the feed is an aqueous methanol solution, and after reconstitution through the first reform stage 18a, the aqueous methanol solution can be recombined into a first reformed atmosphere comprising hydrogen, carbon monoxide, carbon dioxide, and unreacted methanol and water.

The first recombination atmosphere flowing out of the first recombination section 18a may be heated first through the first heat exchanger 16a before entering the first hydrogen permeation membrane section 20a. The hot fluid of the first heat exchanger 16a is, for example, combustion gas generated after combustion of the fuel and air. The temperature of the first recombination atmosphere flowing out from the first recombination section 18a is, for example, 150 degrees Celsius to 350 degrees Celsius, and after being heated by the hot fluid of the first heat exchanger 16a, the temperature thereof can be raised to, for example, 300 to 500 degrees Celsius. .

The first hydrogen permeate membrane section 20a is used to separate hydrogen from the first recombination atmosphere from other products. Since the temperature of the first recombination atmosphere is increased by the hot fluid of the first heat exchanger 16a, the temperature thereof can be raised to 300 to 500 degrees Celsius, and therefore, the temperature of the first recombination atmosphere entering the first hydrogen permeation membrane section 20a does not pass. Low, so it can avoid the problem of thin film hydrogen embrittlement caused by low temperature.

The first product (hydrogen gas, etc.) separated and purified by the first hydrogen filtration membrane section 20a and the first residual gas are respectively sent through different discharge ports. The first product sent from the first hydrogen permeate membrane section 20a can be used for various applications as needed. The fluid (first residual gas) from the first hydrogen permeate membrane section 20a can be used as a reactant for the second recombination section 18b.

The third heat exchanger 16c can provide a cold fluid to cool the fluid (first residual gas) flowing out of the first hydrogen permeating membrane section 20a to lower the temperature before entering the second recombination section 18b. The cold fluid of the third heat exchanger 16c is, for example, air or fuel for the combustion chamber 12, and the temperature thereof is, for example, room temperature to 150 degrees Celsius. The air or fuel used in the combustion chamber 12 or a mixture of the two can achieve the effect of preheating by heat exchange with the first residual gas. In an embodiment, the temperature of the fluid (first residual gas) flowing out from the first hydrogen permeating membrane section 20a is, for example, 300 degrees Celsius to 500 degrees Celsius, and after the temperature is lowered by the third heat exchanger 16c, the temperature may be lowered to 150 degrees Celsius to 350 degrees Celsius.

The second recombination section 18b is for recombining the fluid flowing out of the first hydrogen permeating membrane section 20a and cooled by the third heat exchanger 16c to form a second recombination atmosphere. In an exemplary embodiment, the feed is an aqueous methanol solution, and the first recombination section 18a can recombine the aqueous methanol solution into a first recombination atmosphere comprising hydrogen, carbon monoxide, carbon dioxide, and unreacted methanol and water; the second recombination section 18b can The unreacted aqueous methanol solution of the first recombination stage 18a is recombined into a second recombination atmosphere comprising hydrogen, carbon monoxide, carbon dioxide, and unreacted methanol and water.

The second heat exchanger 16b is for heating the second recombination atmosphere flowing out of the second recombination section 18b. The hot fluid of the second heat exchanger 16b is, for example, combustion gas generated after combustion of the fuel and air. The combustion gas passing through the second heat exchanger 16b first flows through the sixth heat exchanger 16f to carry out the heat exchange before leaving the reformer. The temperature of the second recombination atmosphere flowing out from the second recombination section 18b is, for example, 150 to 350 degrees Celsius, and after being heated by the hot fluid of the second heat exchanger 16b, the temperature thereof can be raised to, for example, 300 to 500 degrees Celsius. .

The second hydrogen permeate membrane section 20b is used to separate hydrogen from the second product in the second recombination atmosphere. Since the second recombination atmosphere is heated by the hot fluid of the second heat exchanger 16b, the temperature thereof can be raised to 300 degrees Celsius to 500 degrees Celsius, and therefore, the temperature of the second recombination atmosphere entering the second hydrogen permeation membrane section 20b does not pass. Low, so it can avoid the problem of thin film hydrogen embrittlement caused by low temperature.

After being filtered by the second hydrogen filtration membrane section 20b, the separated second product and the second residual gas are sent out through different discharge ports. The second product is sent for various applications as required. The temperature of the residual gas filtered by the second hydrogen permeating membrane section 20b (themostmost hydrogen absorbing membrane section) is, for example, 300 to 500 degrees Celsius, which can be performed with air and fuel to be introduced into the combustion chamber 12 The heat exchange achieves the effect of preheating the air and fuel, and it can also be passed into the combustion chamber 12 for combustion after heat exchange.

The combustion chamber 12 is for burning fuel and air to form combustion gas, and supplies thermal energy to the first heat exchanger 16a and the second heat exchanger 16b. In one embodiment, the combustion air or fuel or a mixture of the two may be first passed to the third heat exchanger 16c for heat exchange with the first remaining gas of the first hydrogen permeate membrane section 20a. Alternatively, the combustion air or fuel or a mixture of the two may be passed to the fourth heat exchanger for heat exchange with the second residual gas of the second hydrogen filtration membrane section 20b to achieve the effect of preheating. The first residual gas may be cooled by the third heat exchanger 16c before entering the second recombination section 18b. The second residual gas can then be used to preheat the air and fuel by the fourth heat exchanger 16d.

The sixth heat exchanger 16f can recover the residual heat of the combustion gas for heating, that is, the combustion gas after passing through the combustion gas of the first heat exchanger 16a and the second heat exchanger 16b. The sixth heat exchanger 16f is connected to the air or fuel for combustion or a mixture of the two and the outermost surface of the reactor for heat exchange of the residual heat of the outermost surface of the reactor with air or fuel or a mixture of the two. . Here, the residual heat of the outermost surface of the reactor refers to the combustion gas that has passed through the first heat exchanger and the second heat exchanger, and flows through the flow passage located in the outermost layer of the reactor. The heat provided by the outer casing of the reactor. Since the residual heat of the outermost surface is released to the atmosphere, the heat is recovered by providing the sixth heat exchanger 16f.

The first hydrogen absorbing membrane section 20a and the second hydrogen absorbing membrane section 20b may be a cavity containing a hydrogen absorbing membrane. The material of the hydrogen absorbing membrane may be the same or different, and the material thereof may be a pure metal or a metal alloy, such as pure palladium, palladium silver alloy, palladium copper alloy, vanadium aluminum alloy, vanadium nickel alloy or vanadium palladium alloy. The volume of the first hydrogen permeable membrane section 20a and the second hydrogen permeable membrane section 20b may be the same or different, and the area of the hydrogen absorbing membrane contained therein may be the same or different.

Since the first recombination atmosphere and the second recombination atmosphere are respectively heated by the hot fluid of the first heat exchanger 16a and the second heat exchanger 16b, the first hydrogen permeable membrane section 20a and the second hydrogen permeable membrane section 20b are entered. The temperature can be raised to, for example, 300 degrees Celsius to 500 degrees Celsius. Therefore, when the materials of the first hydrogen filtration membrane section 20a and the second hydrogen filtration membrane section 20b are pure palladium, palladium silver alloy, palladium copper alloy or the like, There is a problem of hydrogen embrittlement, so that good filtration performance can be maintained and the life of the use can be prolonged.

Further, a gas (first product) filtered from the first hydrogen filtration membrane section 20a and a gas (second product) filtered from the second hydrogen filtration membrane section 20b are, for example, hydrogen, water vapor or carbon monoxide, and the temperature thereof is, for example. It is 300 degrees Celsius to 500 degrees Celsius. The first product and the second product may first pass through the methanation section 24 to convert the residual carbon monoxide in the hydrogen to methane, and then to the fifth heat exchanger 16e as a hot fluid for heating the feed. The first residual gas flowing out from the first hydrogen permeating membrane section 20a and the second residual gas flowing out from the second hydrogen permeating membrane section 20b may also pass into the third heat exchanger 16c and the fourth heat exchanger 16d, respectively. As a hot fluid.

In FIG. 1, the first heat exchanger 16a and the second heat exchanger 16b are represented by two separate structures, however, in an embodiment, the first heat exchanger 16a and the second heat exchanger are 16b may also be integrated into a single heat exchanger to increase the temperature of the first recombination atmosphere entering the first hydrogen permeate membrane section 20a and the second hydrogen permeate membrane section 20b and the second recombination atmosphere. Similarly, the third heat exchanger 16c and the fourth heat exchanger 16d are represented by two separate structures, however, in an embodiment, the third heat exchanger 16c and the fourth heat exchanger 16d are also It can be integrated into a single heat exchanger which reduces the temperature of the first remaining gas entering the second recombination section 20b and utilizes the residual heat of the second residual gas to heat the combustion air or fuel or feed. In another embodiment, the first heat exchanger 16a, the second heat exchanger 16b, the third heat exchanger 16c, and the fourth heat exchanger 16d may be integrated into one heat exchange device 16.

Since the separation assisting hydrogen generator of the present invention includes at least two sets of recombination sections and a hydrogen filtration membrane section, the recombination reaction and the membrane separation mechanism can each be in the most appropriate operating temperature range by a repeated procedure. Maintain the performance of the recombination reaction and the life of the hydrogen hydride membrane, while effectively increasing the conversion rate, and obtaining hydrogen with a purity of 90-99.9 vol%.

Since the first recombination atmosphere and the second recombination atmosphere are respectively heated by the hot fluid of the first heat exchanger and the second heat exchanger before entering the first hydrogen filtration membrane segment and the second hydrogen filtration membrane segment, the temperature thereof may be increased. There is no problem of hydrogen embrittlement, so it can maintain good filtration performance and prolong its service life.

Furthermore, the fluid (first residual gas) flowing out of the first hydrogen permeating membrane section is cooled by the cold fluid of the third heat exchanger before flowing into the second recombination section, so that it can be brought to the reconstitution reaction. Operating temperature.

2 is a simplified schematic diagram of various regions in a separation assisted hydrogen generator according to an embodiment of the invention. FIG. 3 is a schematic diagram of a separation assisted hydrogen generator according to an embodiment of the invention.

Referring to FIG. 2 and FIG. 3, the separation assisted hydrogen generator 50 includes a combustion catalyst zone 100, a membrane zone 200, a recombination zone 300, a methanation zone 400, a heat exchange zone 500 and a heat recovery zone 600, between these zones. Separated by flow channels for combustion gas flow.

The combustion catalyst zone 100 is located at the center of the separation assisting hydrogen generator, and the combustion chamber 12 is disposed. The recombination zone 300 is located around the combustion catalyst zone 100, wherein the first recombination section 18a and the second recombination section 18b are disposed. The film region 200 is located between the heavy combustion catalyst region 100 and the recombination zone 300, and is disposed with the first hydrogen absorbing membrane section 20a and the second hydrogen permeable membrane section 20b.

The methanation zone 400 is located outside the recombination zone 300 and is provided with the methanation section 24 described above. The product produced in the membrane zone 200 can enter the methanation zone 400 via a hydrogen gas stream to convert residual carbon monoxide in the hydrogen to methane.

The heat exchange zone 500 is located below the membrane zone 200, the recombination zone 300 and the methanation zone 400, and the heat recovery zone 600. The heat exchange zone 500 includes a first zone 500a and a second zone 500b. The first region 500a is provided with the first heat exchanger 16a and the second heat exchanger 16b. The second zone 500b is provided with the third heat exchanger 16c and the fourth heat exchanger 16d on the periphery of the first zone 500a.

A heat recovery zone 600 is located at the periphery of the methanation zone. In an embodiment, the fifth heat exchanger 16e and the sixth heat exchanger 16f are disposed in the heat recovery zone 600. The fifth heat exchanger 16e is for recovering the waste heat of the product, and the sixth heat exchanger 16f is for recovering the residual heat of the combustion gas for heating. In the present embodiment, the fifth heat exchanger 16e is disposed after the product enters the methanation zone 400. However, in an embodiment, the fifth heat exchanger 16e may also be disposed within the methanation zone 400 or the product enters. Before the methanation zone 400, to reduce the temperature of the methanation zone

Referring to FIG. 2 and FIG. 3, the separation assisting hydrogen generator 50 of the present invention heats the combustion chamber 12 in the central combustion catalyst zone 100, and the generated hot combustion gas first heats the film zone 200 and then reflows. To the recombination zone 300, therefore, the temperature distribution of the separation aid hydrogen generator 50 is sequentially, from high to low, the combustion catalyst zone 100, the membrane zone 200, the recombination zone 300, and the methanation zone 400. In other words, the hot combustion gas may first heat the membrane zone 200 and then heat the recombination zone 300. Before the recombination atmosphere leaves the recombination zone 300 and enters the film zone 200, the hot combustion gas of the first heat exchanger 16a or the second heat exchanger 16b disposed in the first zone 500a of the heat exchange zone 500 is first heated to cause heat combustion. The temperature of the gas is lowered, which is close to the temperature of the recombination zone 300 without excessively heating the recombination zone 300. Before the reaction gas exits the membrane zone 200 and enters the reforming zone 300, it first enters the heat exchange zone 500b, and is cooled by combustion air or a recombination reaction feed, and the feed can also be preheated.

Furthermore, the above-mentioned separation assisting hydrogen generator can be made into various shapes, and the shape thereof can be cylindrical or polygonal. However, the present invention is not limited thereto, and the shape of the separation assisting hydrogen generator can be made according to actual needs. Change and change.

In summary, the separation assisting hydrogen generator of the present invention comprises two stages of recombination section-hydrogen filtration membrane section, thereby effectively increasing the conversion rate, increasing the hydrogen production rate, and the purity of the produced hydrogen is high. The concentration of carbon monoxide is low.

Moreover, the separation assisting hydrogen generator of the present invention separates the membrane zone from the recombination, and only circulates the fluid through the flow channel, and the recombination atmosphere must pass through the heat exchanger before the hydrogenation membrane section of the membrane zone, using heat exchange. The temperature control of the apparatus allows the reformed atmosphere to warm up before entering the hydrogen permeation membrane section, thereby facilitating the life of the hydrogen absorbing membrane.

Furthermore, since the first residual gas passes through the heat exchanger before entering the second recombination section, the temperature is controlled by the heat exchanger, so that the temperature of the first residual gas is lowered to reach a recombination reaction suitable for the second recombination section. Operating temperature.

Although the present invention has been disclosed in the above embodiments, it is not intended to limit the invention, and any one of ordinary skill in the art can make some modifications and refinements without departing from the spirit and scope of the invention. The scope of the invention is defined by the scope of the appended claims.

10, 50. . . Membrane hydrocarbon recombination hydrogen generator

12. . . Combustion chamber

16. . . Heat exchanger unit

16a. . . First heat exchanger

16b. . . Second heat exchanger

16c. . . Third heat exchanger

16d. . . Fourth heat exchanger

16e. . . Fifth heat exchanger

16f. . . Sixth heat exchanger

18. . . Reorganized segment group

18a. . . First reorganization segment

18b. . . Second reorganization segment

20. . . Hydrogen membrane segment

20a. . . First hydrogen membrane segment

20b. . . Second hydrogen membrane segment

twenty four. . . Methanation section

52, 54, 56‧ ‧ flow paths

100‧‧‧Combustion catalytic zone

200‧‧‧film area

300‧‧‧Reorganization area

400‧‧‧ Methanation Zone

500‧‧‧Hot exchange area

500a‧‧‧First District

500b‧‧‧Second District

600‧‧‧heat recovery area

FIG. 1 is a schematic diagram of a separation assisted hydrogen generator according to an embodiment of the invention.

2 is a simplified schematic diagram of various regions in a separation assisted hydrogen generator according to an embodiment of the invention.

FIG. 3 is a schematic diagram of a separation assisted hydrogen generator according to an embodiment of the invention.

10. . . Membrane hydrocarbon recombination hydrogen generator

12. . . Combustion chamber

16. . . Heat exchanger unit

16a. . . First heat exchanger

16b. . . Second heat exchanger

16c. . . Third heat exchanger

16d. . . Fourth heat exchanger

16e. . . Fifth heat exchanger

16f. . . Sixth heat exchanger

18. . . Reorganized segment group

18a. . . First reorganization segment

18b. . . Second reorganization segment

20. . . Hydrogen membrane segment

20a. . . First hydrogen membrane segment

20b. . . Second hydrogen membrane segment

twenty four. . . Methanation section

52, 54, 56. . . Runner

Claims (9)

A separation assisted hydrogen generator comprises: a first recombination section for recombining a feed to form a first recombination atmosphere; and a first hydrogen permeation membrane section for filtering the first recombination atmosphere to form a a first product and a first residual gas; a second recombination section for recombining the first residual gas to form a second recombination atmosphere; and a second hydrogen permeation membrane section for filtering the second recombination atmosphere, Forming a second product and a second residual gas; a first heat exchanger coupled to the first recombination section and the first hydrogen permeate membrane section for heating the feed and receiving the first recombination atmosphere, Heating the first recombination gas stream before entering the first hydrogen filtration membrane section; and a second heat exchanger connected to the second recombination section and the second hydrogen permeation membrane section for receiving the second recombination atmosphere, Heating the second recombination atmosphere before flowing into the second hydrogen permeate membrane section; and a combustion chamber providing heat flow to the first heat exchanger and the second heat exchanger, at least with the first heat exchanger The second heat exchanger is connected, wherein the first recombination section and the first hydrogen permeable membrane section are Separated from each other, the first filter membrane hydrogen separation between the second segment and another segment recombination, the second recombinant segments separated from each other between the second filter and the hydrogen membrane section, and are communicated to the flow passage. The separation assisting hydrogen generator according to claim 1, further comprising a third heat exchanger connected to the combustion chamber, and the same a hydrogen permeable membrane section and the second recombination section are connected to receive the first residual gas, such that the first residual gas enters the second recombination section, and the air or fuel that is introduced into the combustion chamber or both The mixture is heat exchanged. The separation assisting hydrogen generator according to claim 1, further comprising a fourth heat exchanger connected to the second hydrogen filtration membrane section and the combustion chamber for receiving the second residual gas, so that The second residual gas exchanges heat with the air or fuel for combustion of the combustion chamber or a mixture of the two, and is introduced into the combustion chamber. The separation assisted hydrogen generator according to claim 1, further comprising a fifth heat exchanger connecting the first hydrogen filtration membrane segment and the second hydrogen filtration membrane segment and connected to the feed. The first product and the second product are heat exchanged with the feed. The separation assisting hydrogen generator according to claim 4, further comprising a sixth heat exchanger connecting the first heat exchanger and the second heat exchanger and the air or fuel for combustion or both The sixth heat exchanger receives combustion gas passing through the first heat exchanger or the second heat exchanger. The separation assisting hydrogen generator according to claim 5, comprising: a combustion catalyst zone, wherein the combustion chamber is disposed; a recombination zone located around the combustion catalyst zone, and the first recombination section is disposed And the second recombination section; a film zone between the recombination zone and the combustion catalyst zone, the first hydrogen absorbing membrane segment and the second hydrogen permeable membrane segment; a methanation zone located at a periphery of the recombination zone; a heat exchange zone located in the film zone, the recombination zone and the methanation zone or around the methanation zone, the first heat exchanger, the second heat exchanger, and the The third heat exchanger and the fourth heat exchanger described above; and a heat recovery zone located at the periphery of the methanation zone are provided with the fifth and sixth heat exchangers. The separation assisted hydrogen generator of claim 6, wherein the fifth heat exchanger is disposed after the heat recovery zone, the methanation zone, or before the product enters the methanation zone. A separation assisted hydrogen generator comprises: a first recombination section for recombining a feed to form a first recombination atmosphere; and a first hydrogen permeation membrane section for filtering the first recombination atmosphere to form a a first product and a first residual gas; a second recombination section for recombining the first residual gas to form a second recombination atmosphere; and a second hydrogen permeation membrane section for filtering the second recombination atmosphere, Forming a second product and a second residual gas; a combustion chamber for introducing air or fuel or a mixture of the two; and a heat exchange device connected to the combustion chamber and the first hydrogen filtration membrane segment And the second recombination section is connected to receive the first residual gas, so that the first residual gas exchanges heat with the air or fuel or the mixture of the two into the combustion chamber before entering the second recombination section And the second hydrogen a membrane segment connected to receive the second residual gas, to exchange heat between the second residual gas and the air or fuel of the combustion chamber or a mixture of the two, and to pass into the combustion chamber, wherein the first reorganization The segment and the first hydrogen permeable membrane segment are separated from each other, the first hydrogen permeable membrane segment and the second recombination segment are separated from each other, and the second recombination segment and the second hydrogen permeable membrane segment are separated from each other, And connected by flow channels. The separation assisting hydrogen generator according to claim 8 , comprising: a combustion catalyst zone, the combustion chamber is disposed; a recombination zone located around the combustion catalyst zone, and the first recombination section is disposed The second recombination section; a film zone between the recombination zone and the combustion catalyst zone, the first hydrogen permeation membrane segment and the second hydrogen permeation membrane segment; and a methanation zone located outside the recombination zone a heat exchange zone located in the film zone, below or around the recombination zone and the methanation zone, wherein the heat exchange device is disposed; and a heat recovery zone located at the periphery of the methanation zone.