KR102433433B1 - Hydrogen production apparatus - Google Patents

Abstract

The present invention provides a hydrogen production device. According to the hydrogen production device, a heat exchange process, carbon separation, and recovery process for heat recovery are performed simultaneously in one device. Therefore, a process and equipment can be simplified, a maintenance cost can be reduced, and also reaction performance and recovery rates of carbon and hydrogen can be increased. The hydrogen production device comprises: a reactor generating a mixed gas including a hydrogen gas by thermal decomposition of hydrocarbon gas supplied from an outside; and a heat exchange type carbon separation unit having an inner passage, through which the mixed gas discharged from the reactor passes, and an outer passage, through which the hydrocarbon gas supplied to the reactor passes, performing heat exchange between the mixed gas passing through the inner passage and the hydrocarbon gas passing through the outer passage, and at the same time, separating carbon particles included in the mixed gas passing through the inner passage.

Description

Hydrogen production device {HYDROGEN PRODUCTION APPARATUS}

The present invention relates to a hydrogen production device, and more particularly, by allowing a heat exchange process for heat recovery and a carbon separation and recovery process to be performed simultaneously in one device, thereby reducing the simplification and maintenance cost of the process and device, while reducing the reaction performance and performance It relates to a hydrogen production device capable of increasing the recovery rate of carbon and hydrogen.

Hydrogen is widely used as a raw material for chemical products and as a process gas for chemical processes, and its demand is increasing recently as a raw material for fuel cells, a future energy technology. In addition, it is evaluated as an alternative to solve recent environmental problems and problems of rising or exhausting the price of fossil fuels. is in progress

Hydrogen is preferably produced from a renewable energy source in terms of not basically generating carbon dioxide. However, at present, it is economical to manufacture from coal or natural gas, and since it removes a significant portion of carbon dioxide, it also contributes to the purification of fossil fuels.

As a method for producing hydrogen from hydrocarbons, steam reforming method, partial oxidation method, etc. are known, but these existing methods have a problem of causing environmental problems such as global warming because a large amount of carbon dioxide is simultaneously generated.

As another method for producing hydrogen from hydrocarbons, there is a process capable of significantly reducing carbon dioxide emissions by simultaneously producing carbon and hydrogen by thermally decomposing natural gas or heavy oil in a high temperature environment. However, this method requires a very high reaction temperature of 1200 degrees or more, and there is a problem in that a continuous process cannot be performed due to the deposition of the generated carbon.

To this end, there is a catalytic decomposition method using a metal catalyst as a method for lowering the high reaction temperature required for thermal decomposition of hydrocarbons. However, since carbon generated in the catalytic decomposition reaction lowers the activity of the catalyst, there is a problem in that a process of regenerating the metal catalyst using air or steam at a high temperature is additionally required to regenerate the metal catalyst. There is a problem in that the generation of carbon dioxide is further increased.

As a result, in the catalytic pyrolysis process using a metal catalyst, the reaction efficiency can be increased by increasing the inlet temperature of the hydrocarbon gas supplied to the reactor, and the recovery rate of carbon and hydrogen by effectively removing the carbon contained in the reaction gas discharged from the reactor can increase However, only adding the quantity and capacity of the heat exchanger for pre-heating or pre-cooling has a problem in that the process and apparatus become complicated and increase in size, and above all, there is a problem in that the maintenance cost is increased.

For example, when designing a hydrogen production device, a heat exchanger is disposed downstream of the high-temperature reactor to recover thermal energy of exhaust gas discharged from the high-temperature reactor, and the inlet of the high-temperature reactor using the recovered thermal energy It is sometimes used to raise the temperature. However, in this case, the temperature of the exhaust gas passing through the heat exchanger is too low, so that the carbon particles contained in the exhaust gas are agglomerated with each other, thereby accelerating particle formation, causing a problem of sticking to the cooling fins or tubes of the heat exchanger to form scale. Scale deteriorates the performance of the heat exchanger, and eventually causes a problem of clogging the inside of the heat exchanger or causing high pressure loss.

As another example, when designing a hydrogen production device, a heat exchanger is disposed downstream of a carbon separation and recovery device connected to a high-temperature reactor to first separate and recover carbon particles contained in the exhaust gas discharged from the high-temperature reactor, and then remove the carbon particles In some cases, the thermal energy of the exhaust gas is recovered and used to increase the inlet temperature of the high-temperature reactor. However, in this case, since the temperature of the exhaust gas discharged from the high-temperature reactor is at a high temperature of 600 degrees or more, the carbon particles do not agglomerate with each other, so that the efficiency of carbon separation and recovery is lowered. Due to heat loss, there is a problem in that the heat recovery performance of the heat exchanger disposed downstream is deteriorated.

Therefore, while simplifying the process and device and reducing maintenance costs, the heat recovery process is performed at a high temperature condition, and the carbon separation and recovery process is performed at a low temperature condition, thereby increasing the recovery rate of generated carbon and hydrogen. A hydrogen production device with a new structure is required.

Republic of Korea Patent Publication No. 1353719 (2014.02.11. Announcement)

An object of the present invention for solving the above-described problems is to allow the heat exchange process for heat recovery and the carbon separation and recovery process to be performed simultaneously in one device, thereby reducing the simplification and maintenance cost of the process and the device while reducing the reaction performance and carbon And to provide a hydrogen production device capable of increasing the recovery rate of hydrogen.

In addition, an object of the present invention is to increase the recovery rate of atomized carbon particles by performing a pre-cooling process when separating carbon particles contained in hydrogen gas using the cooling and heat energy of hydrocarbon gas supplied to the reactor, and hydrogen gas discharged from the reactor An object of the present invention is to provide a hydrogen production device capable of increasing the reaction performance of the reactor by allowing the hydrocarbon gas supplied to the reactor to undergo a preheating process using the thermal energy of the reactor.

Hydrogen production apparatus according to an embodiment of the present invention for solving the above problems, a reactor for generating a mixed gas including hydrogen gas by thermal decomposition of hydrocarbon gas supplied from the outside; and an inner passage through which the mixed gas discharged from the reactor passes, and an outer passage through which the hydrocarbon gas supplied to the reactor passes, and heat exchange between the mixed gas passing through the inner passage and the hydrocarbon gas passing through the outer passage; At the same time, it characterized in that it comprises a; heat exchange type carbon separation unit for separating the carbon particles contained in the mixed gas passing through the inner flow path.

In the hydrogen production apparatus according to this embodiment, the heat exchange type carbon separation unit forms the inner flow path therein, and induces a cyclonic flow of the mixed gas passing through the inner flow path to separate carbon particles included in the mixed gas and an inner chamber for the purpose of The hydrocarbon gas passing through may be preheated and supplied to the reactor, and the mixed gas passing through the inner channel may be pre-cooled by the cooling energy of the hydrocarbon gas passing through the outer channel.

In the hydrogen production apparatus according to this embodiment, the heat exchange type carbon separation unit is a first preheating hydrocarbon gas supplied from the hydrocarbon gas supply unit, and the first separation of carbon particles contained in the mixed gas discharged from the reactor The first heat exchange type carbon separation unit and the first heat exchange type carbon separation unit are connected to the first heat exchange type carbon separation unit, and the hydrocarbon gas discharged from the first heat exchange type carbon separation unit is preheated for secondary preheating and supplied to the reactor, and the first heat exchange type carbon It may include a second heat exchange type carbon separation unit for secondary separation of residual carbon particles contained in the mixed gas discharged from the separation unit.

In the hydrogen production apparatus according to this embodiment, the inner chamber has a first inner flow path through which the mixed gas discharged from the reactor is introduced, and induces a cyclonic flow of the mixed gas passing through the first inner flow path to be mixed It has a first inner chamber for primary separation of carbon particles contained in gas, and a second inner passage through which the mixed gas discharged from the first inner chamber is introduced, and a cyclonic flow of the mixed gas passing through the second inner passage. to induce a second inner chamber for secondary separation of carbon particles contained in the mixed gas.

In the hydrogen production apparatus according to this embodiment, a carbon recovery unit for recovering the carbon particles discharged from the heat exchange type carbon separation unit; may further include, in this case, the carbon recovery unit is a filter for collecting carbon particles can

In the hydrogen production apparatus according to this embodiment, an unreacted gas separator for separating unreacted hydrocarbon gas contained in the hydrogen gas discharged from the heat exchange type carbon separator; may further include.

In the hydrogen production apparatus according to this embodiment, it is installed on the hydrocarbon gas stream connecting the heat exchange type carbon separation unit and the reactor, and the hydrocarbon gas discharged from the heat exchange type carbon separation unit and the unreacted gas separator It may further include; a gas mixing unit for mixing the separated unreacted hydrocarbon gas.

In the hydrogen production apparatus according to the present embodiment, the heat exchange type carbon separation unit may further include a flow guide member disposed in the outer flow path to promote heat exchange between the mixed gas and the hydrocarbon gas.

In the hydrogen production apparatus according to this embodiment, the flow guide member may be arranged in a spiral shape from a lower region of the outer passage through which hydrocarbon gas is introduced to an upper region of the outer passage through which hydrocarbon gas is discharged.

In the hydrogen production apparatus according to this embodiment, the flow guide member may have at least one of holes, grooves and protrusions formed on the surface so as to promote convective heat exchange of hydrocarbon gas moving along the outer flow path.

In the hydrogen production apparatus according to this embodiment, the flow guide member is formed to extend from a lower region of the outer passage through which hydrocarbon gas is introduced toward an upper region of the outer passage through which hydrocarbon gas is discharged, A plurality may be provided while maintaining uniform intervals along the circumferential direction.

In the hydrogen production apparatus according to this embodiment, the flow guide member is disposed in the lower region of the outer flow path, and is disposed in an upper region of the outer flow path and an inner lower flow channel extending obliquely toward the upper side. , it may include an inner portion of the upper flow while going to the upper side and extending vertically.

According to the present invention, since the heat exchange type carbon separator capable of simultaneously performing heat exchange for pre-cooling and pre-heating together with the separation action of the gas to be treated is used, the size and process of the device can be simplified, and energy consumed in the process can be reduced. You can save a lot.

According to the present invention, a heat exchange type carbon separation unit having an inner chamber for a cyclone effect and an outer chamber for a heat exchange effect is used to perform a pre-cooling process when the carbon particles are separated using the cooling and heat energy of the hydrocarbon gas supplied to the reactor. Therefore, it is possible to greatly increase the recovery rate by accelerating the particleization of atomized carbon.

According to the present invention, since the heat recovery is performed simultaneously with the carbon separation and recovery of the mixed gas discharged from the reactor through the heat exchange type carbon separation unit, it is possible to suppress the formation of scale of carbon particles in the heat exchange process.

1 is an exemplary view showing a hydrogen production apparatus according to a first embodiment of the present invention.
2 is a side view illustrating a heat exchange type carbon separator according to a first embodiment of the present invention.
3 is a partial cross-sectional perspective view of a heat exchange type carbon separation unit according to a second embodiment of the present invention.
4 is an exemplary side view of the heat exchange type carbon separation unit of FIG. 3 .
5 is a partial cross-sectional perspective view of a heat exchange type carbon separation unit according to a third embodiment of the present invention.
6 is an exemplary cross-sectional view taken along lines AA and BB of FIG. 5 .
7 is an exemplary view showing a heat exchange type carbon separator according to a fourth embodiment of the present invention.
8 is an exemplary view showing a heat exchange type carbon separator according to a fifth embodiment of the present invention.

Hereinafter, preferred embodiments of the present invention in which the above-described problems to be solved can be specifically realized will be described with reference to the accompanying drawings. In describing the present embodiments, the same names and reference numerals may be used for the same components, and an additional description thereof may be omitted.

1 is an exemplary view showing a hydrogen production apparatus according to a first embodiment of the present invention.

Referring to FIG. 1 , the hydrogen production apparatus according to this embodiment includes a reactor 100 , a hydrocarbon gas supply unit 200 , a heat exchange type carbon separation unit 300 , a carbon recovery unit 400 , and a hydrogen gas storage unit 500 . may include.

The reactor 100 may pyrolyze hydrocarbon gas supplied from the outside through a chemical reaction to generate a mixed gas including hydrogen gas.

As the hydrocarbon gas, natural gas (NG) containing hydrocarbons, liquefied natural gas (LNG), naphtha, etc. may be used. The hydrocarbon gas may generate a mixed gas including hydrogen and carbon while passing through the reactor 100 .

The reactor 100 may be a catalytic pyrolysis reactor.

The catalytic pyrolysis reactor 100 may include a heater 110 , and an external heating method using the heater 110 disposed outside the reaction space may be applied. A high-temperature environment may be created inside the reactor 100 through the heater 110, and the hydrocarbon gas introduced into the reactor 100 may be pyrolyzed in a high-temperature environment to be decomposed into hydrogen and carbon.

In addition, the catalytic pyrolysis reactor 100 may include a metal catalyst 120 , and the pyrolysis reaction of hydrocarbon gas may be promoted through the metal catalyst 120 disposed inside the reaction space. The metal catalyst 120 may lower the reaction temperature (700 to 1200 degrees) of the hydrocarbon-based hydrocarbon gas to be thermally decomposed, and a noble metal catalyst such as nickel, iron, platinum, or the like may be used as the metal catalyst 120 .

As such, since the reaction temperature (700 to 1200 degrees) of the reactor 100 can be relatively lowered by the metal catalyst 120 compared to the case where the catalyst is not used, the reaction rate in the reactor 100 can be increased, As the heat source 130 of the heater 110 , renewable energy such as solar heat, geothermal heat, and wind power may be utilized.

The hydrocarbon gas supply unit 200 may be connected to the heat exchange type carbon separation unit 300 through the first stream S1 which is a hydrocarbon gas stream, and may supply hydrocarbon gas to the heat exchange type carbon separation unit 300 . Thereafter, the hydrocarbon gas passing through the heat exchange type carbon separation unit 300 may be supplied to the reactor 100 through the second stream S2 .

And, the hydrogen production apparatus may further include a hydrocarbon gas flow rate control unit 210 , the hydrocarbon gas flow rate control unit 210 may be installed on the first stream S1 , and in the hydrocarbon gas supply unit 200 . It is possible to adjust the flow rate of the hydrocarbon gas supplied to the heat exchange type carbon separation unit (300). A valve may be used as the hydrocarbon gas flow rate control unit 210 .

The heat exchange type carbon separation unit 300 may be installed on a stream connecting the reactor 100 , the hydrocarbon gas supply unit 200 , the carbon recovery unit 400 , and the hydrogen gas storage unit 500 . The heat exchange type carbon separator 300 can separate hydrogen gas and carbon particles in the mixed gas discharged from the reactor 100, and pre-cool the mixed gas in the separation process of carbon particles to accelerate carbon particleization. The recovery rate of particles may be increased, and the inlet temperature of the reactor 100 may be increased by preheating the passing hydrocarbon gas. The heat exchange type carbon separation unit 300 will be described later in detail.

The carbon recovery unit 400 may be connected to the heat exchange type carbon separation unit 300 through the fourth stream S4 that is a carbon stream, and may recover carbon particles separated and discharged from the heat exchange type carbon separation unit 300 . .

A filter for collecting carbon particles may be used as the carbon recovery unit 400 , and in this case, the carbon recovery unit 400 may be installed in the fourth stream S4 .

And, the hydrogen production apparatus may further include a negative pressure generator 410, the negative pressure generator 410 may be connected to the heat exchange type carbon separation unit 300 and the fourth stream (S4), the fourth stream ( It is possible to provide a conveying pressure of S4).

In addition, the hydrogen production apparatus may further include a conveying pressure control unit 420, the conveying pressure control unit 420 may be installed on the fourth stream (S4), acting on the fourth stream (S4) Feed pressure can be adjusted and set. A valve may be used as the transfer pressure adjusting unit 420 .

The hydrogen gas storage unit 500 may be connected to the heat exchange type carbon separation unit 300 through a fifth stream S5 that is a hydrogen stream, and may store the hydrogen gas separated and discharged from the heat exchange type carbon separation unit 300 . .

In addition, the hydrogen production apparatus may further include a gas analyzer 600 and an unreacted gas separator 700 .

The gas analyzer 600 may be installed on the fifth stream S5 and may measure the concentration of unreacted hydrocarbon gas contained in the hydrogen gas separated and discharged from the heat exchange type carbon separation unit 300 .

The unreacted gas separator 700 may be installed downstream of the gas analyzer 600 on the fifth stream S5, and the unreacted hydrocarbon gas contained in the hydrogen gas separated and discharged from the heat exchange type carbon separator 300. can be separated, and thus, high-purity hydrogen gas can be obtained.

For example, the concentration value of the unreacted hydrocarbon gas present in the hydrogen gas transferred along the fifth stream S5 through the gas analyzer 600 exceeds a preset reference value, so the desired purity (concentration) of the hydrogen gas is not satisfied. Otherwise, the unreacted gas separator 700 may separate the unreacted hydrocarbon gas present in the hydrogen gas, and store high-purity hydrogen gas from which the unreacted hydrocarbon gas is removed in the hydrogen gas storage unit 500 .

Of course, in the hydrogen production apparatus, the hydrogen gas storage unit 500 described above may be excluded depending on the place where the produced hydrogen gas is used. That is, the hydrogen gas discharged from the heat exchange type carbon separation unit 300 may be directly used as a heat source at the place of use.

In addition, in the hydrogen production apparatus, the gas analyzer 600 and the unreacted gas separator 700 described above may be excluded depending on the place where the produced hydrogen gas is used. That is, the hydrogen gas including the unreacted hydrocarbon gas discharged from the heat exchange type carbon separation unit 300 may be directly used as a heat source at the place of use without a separate purification process.

Meanwhile, the unreacted gas separator 700 may be connected to the second stream S2, which is a hydrocarbon gas stream, through the bypass stream S6, and the unreacted hydrocarbon gas separated in the unreacted gas separator 700 is bypassed. It may be joined to the second stream S2 through the stream S6. That is, the unreacted hydrocarbon gas separated in the unreacted gas separator 700 may be re-supplied to the reactor 100 .

In addition, the hydrogen production apparatus may further include a gas mixing unit 800, the gas mixing unit 800 is installed on the second stream (S2) and the hydrocarbon gas discharged from the heat exchange type carbon separation unit 300 and The unreacted hydrocarbon gas separated and discharged from the unreacted gas separator 700 may be mixed, and then the mixed hydrocarbon gas may be supplied to the reactor 100 .

In addition, the hydrogen production apparatus may further include a heat exchange unit 900 , the heat exchange unit 900 may be installed on a fifth stream S5 that is a hydrogen gas stream. That is, the heat exchange unit 900 may use the hydrogen gas flowing in the fifth stream S5 as a refrigerant to heat the external use water, and the heated used water may be used in various places. In this way, when the heat exchange unit 900 is applied, since the temperature of the hydrogen gas stored in the hydrogen gas storage unit 500 can be lowered, the loss of the hydrogen gas stored in the hydrogen gas storage unit 500 can be reduced.

2 is a side view illustrating a heat exchange type carbon separator according to a first embodiment of the present invention.

1 and 2 , the heat exchange type carbon separation unit 300 may basically separate hydrogen gas and carbon particles in the mixed gas discharged to the reactor 100 . In addition, the heat exchange type carbon separation unit 300 pre-cools the mixed gas in the separation process of the carbon particles to accelerate the carbonization, so that the recovery rate of the carbon particles can be increased. In addition, the heat exchange type carbon separator 300 preheats the hydrocarbon gas supplied to the reactor 100 to increase the inlet temperature of the reactor 100 , so that the reaction efficiency in the reactor 100 can be greatly increased.

Specifically, first, the heat exchange type carbon separation unit 300 may be connected to the hydrocarbon gas supply unit 200 as a first stream (S1), and the hydrocarbon gas supplied from the hydrocarbon gas supply unit 200 is supplied to the reactor 100. It may pass through the heat exchange type carbon separation unit 300 first.

In addition, the heat exchange type carbon separation unit 300 may be connected to the reactor 100 as a second stream (S2), and the hydrocarbon gas discharged from the heat exchange type carbon separation unit 300 passes through the second stream S2 to the reactor. (100) can be supplied.

In addition, the heat exchange type carbon separation unit 300 may be connected to the reactor 100 as a third stream (S3), and the mixed gas discharged from the reactor 100 passes through the third stream (S3) to the heat exchange type carbon separation unit (300) can be supplied.

In addition, the heat exchange type carbon separation unit 300 may be connected to the negative pressure generating unit 410 as a fourth stream (S4), and the carbon particles separated and discharged from the heat exchange type carbon separation unit 300 are the fourth stream (S4). It may be recovered by the carbon recovery unit 400 installed on it.

In addition, the heat exchange type carbon separation unit 300 may be connected to the hydrogen gas storage unit 500 as a fifth stream (S5), and the hydrogen gas separated and discharged from the heat exchange type carbon separation unit 300 is a fifth stream (S5). ) through the hydrogen gas storage unit 500 may be stored.

When the heat exchange type carbon separation unit 300 separates the hydrogen gas and carbon particles in the mixed gas discharged to the reactor 100, the hydrocarbon gas supplied to the reactor 100 is preheated by using the thermal energy of the mixed gas. The inlet temperature of the reactor 100 can be increased, and the carbon particles recovered by the carbon recovery unit 400 can be recovered by pre-cooling the mixed gas when the mixed gas is separated by using the cooling heat energy of the hydrocarbon gas to accelerate the carbonization. can increase

To this end, the heat exchange type carbon separation unit 300 may include an inner chamber 310 and an outer chamber 320 .

The inner chamber 310 may separate hydrogen gas and carbon particles contained in the mixed gas discharged from the reactor 100 .

The inner chamber 310 may have an inner flow path 311 into which the mixed gas discharged from the reactor 100 is introduced. The inner flow path 311 may have a cylindrical structure of upper and lower narrows.

In addition, the inner chamber 310 may have a mixed gas inlet 312 connecting the third stream S3 and the upper portion of the inner passage 311 , and the mixed gas inlet 312 is the center of the inner passage 311 . It can be arranged on one side eccentric in. Accordingly, the mixed gas flowing into the inner flow path 311 through the mixed gas inlet 312 may generate a cyclonic flow that slowly descends while turning with respect to the center of the inner flow path 311 .

Due to this cyclone flow, a relatively light hydrogen gas among the mixed gases may flow upwards of the inner passage 311 , and relatively heavy carbon particles may flow downwards of the inner passage 311 .

In addition, the inner chamber 310 may have a carbon outlet 313 connecting the fourth stream S4 and the lower portion of the inner flow path 311 , and the carbon particles separated in the inner channel 311 are separated from the carbon outlet 313 . ) may be transferred to the fourth stream S4.

In addition, the inner chamber 310 may have a hydrogen gas outlet 314 connecting the fifth stream S5 and the upper portion of the inner passage 311 , and the hydrogen gas separated in the inner passage 311 is a hydrogen gas outlet It may be transferred to the fifth stream S5 through 314 .

A material having excellent heat transfer may be used as the inner chamber 310 . That is, the warm energy of the mixed gas in contact with the inner surface may be transferred to the outer surface, and the cooling energy of the hydrocarbon gas in contact with the outer surface may be transferred to the inner surface. Also, although not shown, radiating fins may be protruded from the outer surface of the inner chamber 310 to increase the heat exchange area.

The outer chamber 320 may preheat the hydrocarbon gas supplied to the reactor 100 by way of the hydrocarbon gas transferred from the hydrocarbon gas supply unit 200 to the reactor 100 .

The outer chamber 320 may be disposed to surround the inner chamber 310 , and an outer flow path 321 may be formed between the outer chamber 310 and the inner chamber 310 . That is, the outer flow path 321 may be formed by the outer surface of the inner chamber 310 and the inner surface of the outer chamber 320 .

In addition, the outer chamber 320 may have a hydrocarbon gas inlet 322 connecting the first stream S1 and the lower portion of the outer flow path 321, and the hydrocarbon gas transferred along the first stream S1 is hydrocarbon. The gas may be transferred to a lower portion of the outer flow path 321 through the gas inlet 322 .

In addition, although not shown, the outer chamber 320 may have a flow diffusion member on the bottom surface. The flow diffusion member can evenly spread the hydrocarbon gas flowing into the center of the lower region of the outer passage 321 through the hydrocarbon gas inlet 322 to the peripheral region of the outer passage 321 . That is, the hydrocarbon gas flowing into the center of the lower region of the outer flow path 321 through the hydrocarbon gas inlet 322 by the flow diffusion member may be uniformly distributed to surround the inner chamber 310 .

In addition, the outer chamber 320 may have a hydrocarbon gas outlet 323 connecting the second stream S2 and the upper portion of the outer passage 321, and the hydrocarbon gas passing through the outer passage 321 is a hydrocarbon gas outlet. It may be transferred to the second stream S2 through 323 .

A material having excellent thermal insulation may be used as the outer chamber 320 , and a thermal insulation cover may be further provided on the outer surface of the outer chamber 320 .

As such, the thermal energy of the mixed gas flowing in the inner passage 311 may be transferred to the outer passage 321 through the inner chamber 310 , and the cooling and heat energy of the hydrocarbon gas flowing in the outer passage 321 is the inner It may be transmitted to the inner flow path 311 through the chamber 310 . Due to this heat exchange, the temperature of the mixed gas flowing in the inner passage 311 may be decreased, and the temperature of the hydrocarbon gas flowing in the outer passage 321 may be increased.

As a result, the hydrocarbon gas supplied from the hydrocarbon gas supply unit 200 is preheated by the thermal energy of the mixed gas passing through the inner passage 311 while passing through the outer passage 321 to the reactor 100 in a state where the temperature is increased. can be supplied, and since the inlet temperature of the reactor 100 can be increased, the reaction efficiency can be increased. In addition, since a separate heat exchanger for preheating the hydrocarbon gas supplied to the reactor 100 may be excluded, the process and apparatus may be simplified, and maintenance costs may be reduced.

In addition, the mixed gas discharged from the reactor 100 is pre-cooled by the cooling and heat energy of the hydrocarbon gas passing through the outer passage 321 during the cyclone flow in the inner passage 311, so that the atomized carbon is aggregated with each other and particle formation is accelerated. can Accordingly, the recovery rate of the carbon particles collected by the carbon recovery unit 400 of the filter structure may be increased. In addition, since a separate heat exchanger for cooling the mixed gas may be excluded, the process and apparatus may be simplified, and maintenance costs may be reduced.

Meanwhile, FIG. 3 is a partial cross-sectional perspective view of a heat exchange type carbon separation unit according to a second embodiment of the present invention, and FIG. 4 is an exemplary side view of the heat exchange type carbon separation unit of FIG. 3 .

3 and 4 , the heat exchange type carbon separation unit 300 according to the present embodiment may further include a flow guide member 330 .

The flow guide member 330 may be disposed in the outer passage 321 , and may increase heat exchange efficiency between the hydrocarbon gas flowing in the outer passage 321 and the mixed gas flowing in the inner passage 311 .

The flow guide member 330 may be arranged in a spiral shape on the outer flow path 321 , and the outer flow guide member 330 may have a spiral flow path by the flow guide member 330 . Specifically, the flow guide member 330 may be coupled to the outer surface of the inner chamber 310, and the hydrocarbon gas outlet 323 is connected in the lower region of the outer flow path 321 to which the hydrocarbon gas inlet 322 is connected. It may be arranged in a spiral shape while going to the upper region of the outer flow path 321 to be used.

Accordingly, while the hydrocarbon gas flowing in from the hydrocarbon gas inlet 322 slowly moves along the spiral-shaped outer flow path 321 surrounding the inner chamber 310, sufficient time is left before being discharged from the hydrocarbon gas outlet 323. It may exchange heat with the inner chamber 310 . As a result, the hydrocarbon gas introduced into the lower region of the outer passage 321 flows in a spiral shape toward the upper region of the outer passage 321 while in contact with the spiral-shaped flow guide member 330, and the flow time may be delayed. Thereby, more effective heat exchange can be achieved in the entire area of the outer flow path 321 .

5 is a partial cross-sectional perspective view of a heat exchange type carbon separation unit according to a third embodiment of the present invention, and FIG. 6 is an exemplary cross-sectional view taken along lines A-A and B-B of FIG. 5 .

5 and 6 , the flow guide member 330 ″ according to the present embodiment may be coupled to the outer surface of the inner chamber 310 , and uniformly spaced along the circumferential direction of the inner chamber 310 . A plurality of flow guides may be provided. Therefore, the outer flow path 321 may be divided into a plurality of flow spaces by the plurality of flow guide members 330 ″. Then, the hydrocarbon gas flowing into the center of the lower region of the outer passage 321 through the hydrocarbon gas inlet 322 is evenly spread to the peripheral region of the outer passage 321 by the flow diffusion member, and then the flow guide member 330 The flow may be evenly distributed toward the plurality of outer flow passages 321 partitioned by ").

In addition, the flow guide member 330 ″ may include an upper flow inner portion 331 and a lower flow guide inner portion 332 .

The upper flow passage inner 331 may be disposed in an upper region of the outer flow passage 321 , the lower flow passage inner 332 may be disposed in a lower region of the outer flow passage 321 , and the upper flow passage inner 331 . ) and the inner part 332 during the lower flow can be installed separately.

That is, during the upper flow, the inner 331 extends vertically from the lower region of the outer passage 321 adjacent to the hydrocarbon gas inlet 322 toward the upper region of the outer passage 321 adjacent to the hydrocarbon gas outlet 323. can Accordingly, the hydrocarbon gas can be vertically flow guided to the upper region of the outer flow passage 321 toward the hydrocarbon gas outlet 323 while being in contact with the inner 331 during the upper flow.

The inner portion 332 during the lower flow is inclined from the lower region of the outer passage 321 adjacent to the hydrocarbon gas inlet 322 to the upper portion of the outer passage 321 adjacent to the hydrocarbon gas outlet 323. Accordingly, the flow time may be delayed while the hydrocarbon gas flows obliquely to the upper region of the outer flow passage 321 while in contact with the inner 332 during the lower flow.

Of course, unlike the one shown, the flow guide member 330" may be composed of only the upper flow passage inner 331 forming a vertical flow path, and only the lower flow passage inner 332 forming an obliquely inclined flow path. it might be

Preferably, in the lower region of the outer flow path 321 adjacent to the hydrocarbon gas inlet 322 and having a relatively large area due to the reduced cross-sectional shape of the inner chamber 310, the lower portion of the inner chamber 332 during the lower flow. may be disposed, adjacent to the hydrocarbon gas outlet 323 and in the upper region of the outer flow passage 321 in which the passage of a relatively narrow area is secured due to the enlarged cross-sectional shape of the inner chamber 310, the inner ( 331) can be arranged.

For example, as shown in Fig. 6 (a), the inner portion 332 during the lower flow passage may be formed obliquely from the lower end to the upper end, and may be arranged to have a relatively small amount along the circumferential direction of the outer passage 321. can During this lower flow, the inner 332 delays the flow time of the hydrocarbon gas so that heat exchange is effectively performed, so that the temperature of the hydrocarbon gas introduced into the outer flow passage 321 can be rapidly increased, and the lower portion of the inner flow passage 311 is formed. It is possible to effectively cool the temperature of the mixed gas that implements a strong cyclonic flow in the region.

In addition, as shown in FIG. 6 (b), the inner portion 331 during the upper flow may be formed vertically from the lower end to the upper end, and may be disposed to have a relatively large quantity along the circumferential direction of the outer passage 321. can The inner 331 during the upper flow ensures sufficient heat exchange with the hydrocarbon gas until just before being discharged through the hydrocarbon gas outlet 323, and at the same time guides the vertical flow of the hydrocarbon gas toward the hydrocarbon gas outlet 323 to guide the hydrocarbon gas. It is possible to reduce the pressure loss of the hydrocarbon gas discharged from the gas outlet 323 .

In addition, due to the relatively small amount of the lower flow inner portion 332 and the relatively large amount of the upper flow inner portion 331 , the hydrocarbon gas flowing from the lower region to the upper region of the outer flow passage 321 is lower flow. Convection heat exchange may be promoted while being dispersed and diffused again in the boundary region between the guide portion 332 and the inner portion 331 during the upper flow.

As such, according to the shape of the inner chamber 310 and the outer chamber 320 and the required inlet temperature of the reactor 100, the flow guide members 330 and 330 "can be appropriately changed in quantity, shape and arrangement structure, Accordingly, effective heat exchange between the mixed gas flowing in the inner passage 311 and the hydrocarbon gas flowing in the outer passage 321 can be achieved.

On the other hand, the flow guide members 330 and 330" may have through holes, grooves or protrusions formed on the surface. These through holes, grooves or protrusions are turbulent flow of hydrocarbon gas flowing along the surface of the flow guide members 330 and 330". By activating the convective heat exchange in the entire area of the outer flow path 321 may be further activated.

Meanwhile, FIG. 7 is an exemplary view showing a heat exchange type carbon separation unit according to a fourth embodiment of the present invention.

Referring to FIG. 7 , the heat exchange type carbon separation unit 3000 according to the present embodiment is distinguished from the above-described embodiment in that it has a multi-stage heat exchange type carbon separation unit.

Specifically, the multi-stage heat exchange type carbon separation unit 3000 according to the present embodiment may include a first heat exchange type carbon separation unit 3100 and a second heat exchange type carbon separation unit 3200 . In this case, the first heat exchange type carbon separation unit 3100 and the second heat exchange type carbon separation unit 3200 may be configured in the same manner as the heat exchange type carbon separation unit 300 according to the above-described embodiment, respectively.

The first heat exchange type carbon separation unit 3100 performs primary heat exchange between the cold energy of the hydrocarbon gas supplied from the hydrocarbon gas supply unit 200 and the warm energy of the mixed gas discharged to the reactor 100, and the hydrocarbon gas supply unit 200 ), the hydrocarbon gas supplied from the may be preheated first, and carbon particles contained in the mixed gas discharged from the reactor 100 may be first separated.

In addition, the second heat exchange type carbon separation unit 3200 is connected to the downstream of the first heat exchange type carbon separation unit 3100, and is primarily preheated in the first heat exchange type carbon separation unit 3100. Hydrocarbons discharged from the first heat exchange type carbon separation unit 3100 through secondary heat exchange between the cold heat energy and the warm heat energy of the mixed gas discharged after the carbon particles are first separated by the first heat exchange type carbon separation unit 3100 The gas may be preheated to the reactor 100 and supplied to the reactor 100 , and the remaining carbon particles included in the mixed gas discharged from the first heat exchange type carbon separation unit 3100 may be secondarily separated.

As such, if the multi-stage heat exchange type carbon separation unit 3000 is provided, the inlet temperature of the hydrocarbon gas supplied to the reactor 100 can be further increased, and the carbon recovery rate in the carbon recovery unit 400 and the hydrogen gas storage unit 500 ) can further increase the hydrogen recovery rate.

As shown, the capacity of the first heat exchange type carbon separation unit 300 and the capacity of the second heat exchange type carbon separation unit 300 are the same as each other, but the capacity of the second heat exchange type carbon separation unit 300 is It may be designed to be smaller than the capacity of the first heat exchange type carbon separation unit 300 .

8 is an exemplary view showing a heat exchange type carbon separator according to a fifth embodiment of the present invention.

Referring to FIG. 8 , the heat exchange type carbon separation unit 3000 ″ according to the present embodiment is distinguished from the above-described embodiment in that it has a multi-stage inner chamber.

Specifically, the heat exchange type carbon separation unit 3000 ″ according to the present embodiment may include a first inner chamber 3310 , a second inner chamber 3320 , and an outer chamber 3330 .

The first inner chamber 3310 has a first inner flow path 3311 through which the mixed gas discharged from the reactor 100 is introduced, and induces a cyclonic flow of the mixed gas passing through the first inner flow path 3311 to induce a mixed gas. It is possible to primary separation of the carbon particles contained in the.

The second inner chamber 3320 has a second inner flow path 3321 through which the mixed gas discharged from the first inner chamber 3310 is introduced, and induces a cyclonic flow of the mixed gas passing through the second inner flow path 3321 . Thus, the carbon particles contained in the mixed gas can be secondarily separated.

In this case, the outer chamber 3330 may be disposed to surround the first inner chamber 3310 and the second inner chamber 3320 , and may be disposed between the first inner chamber 3310 and the second inner chamber 3320 on the outside. A flow path 3331 may be formed.

As such, if a multi-stage inner chamber is provided inside one outer chamber 3330 , the inlet temperature of the hydrocarbon gas supplied to the reactor 100 can be further increased, and the carbon recovery rate and hydrogen gas in the carbon recovery unit 400 . It is possible to further increase the hydrogen recovery rate in the storage unit 500 .

As described above, the hydrogen production apparatus according to the present invention uses the heat exchange type carbon separation unit 300 having an inner chamber 310 for a cyclone effect and an outer chamber 320 for a heat exchange effect, the reactor 100 Since the carbon particles undergo a pre-cooling process when separating the carbon particles by using the cooling energy of the hydrocarbon gas supplied to the ) so that the hydrocarbon gas supplied to the reactor 100 undergoes a preheating process using the thermal energy of the mixed gas discharged from the .

In addition, since the hydrogen production device according to the present invention uses the heat exchange type carbon separation unit 300 of the dual flow path capable of simultaneously performing heat exchange for pre-cooling and pre-heating together with the separation action of the gas to be treated, the size and process of the device can be simplified, and the energy consumed in the process can be greatly reduced.

Although the preferred embodiment of the present invention has been described with reference to the drawings as described above, those skilled in the art may vary the present invention in various ways without departing from the spirit and scope of the present invention as set forth in the following claims. may be modified or changed.

100: reactor
300: heat exchange type carbon separation unit
310: inner chamber
320: outer chamber

Claims (12)

a reactor that pyrolyzes hydrocarbon gas supplied from the outside to generate a mixed gas including hydrogen gas; and
It has an inner passage through which the mixed gas discharged from the reactor passes and an outer passage through which the hydrocarbon gas supplied to the reactor passes, and at the same time as heat exchange between the mixed gas passing through the inner passage and the hydrocarbon gas passing through the outer passage. , a heat exchange type carbon separation unit for separating carbon particles contained in the mixed gas passing through the inner flow path;
The heat exchange type carbon separation unit forms the inner flow path therein, and induces a cyclone flow of the mixed gas passing through the inner flow path to separate the carbon particles contained in the mixed gas, and surrounds the inner chamber. and an outer chamber disposed to form the outer flow path between the inner chamber and the inner chamber,
The hydrocarbon gas passing through the outer channel is preheated by the warm energy of the mixed gas passing through the inner channel and supplied to the reactor, and the mixture passing through the inner channel by the cooling energy of the hydrocarbon gas passing through the outer channel Hydrogen production device, characterized in that the gas is pre-cooled. delete According to claim 1,
The heat exchange type carbon separation unit,
A first heat exchange type carbon separation unit for preheating the hydrocarbon gas supplied from the hydrocarbon gas supply unit and first separating carbon particles contained in the mixed gas discharged from the reactor;
It is connected to the first heat exchange type carbon separation unit, and the hydrocarbon gas discharged from the first heat exchange type carbon separation unit is preheated for secondary preheating and supplied to the reactor, and the mixed gas discharged from the first heat exchange type carbon separation unit is supplied to the reactor. Hydrogen production apparatus comprising a second heat exchange type carbon separation unit for secondary separation of the contained residual carbon particles. According to claim 1,
The inner chamber,
A first inner chamber having a first inner flow path through which the mixed gas discharged from the reactor is introduced, and for inducing a cyclone flow of the mixed gas passing through the first inner channel to first separate carbon particles contained in the mixed gas; ,
a second inner flow path through which the mixed gas discharged from the first inner chamber is introduced, and inducing a cyclonic flow of the mixed gas passing through the second inner flow path to secondaryly separate carbon particles contained in the mixed gas Hydrogen production apparatus comprising an inner chamber. According to claim 1,
Further comprising; a carbon recovery unit for recovering the carbon particles discharged from the heat exchange type carbon separation unit;
The carbon recovery unit is a hydrogen production device, characterized in that the filter for collecting carbon particles. According to claim 1,
Hydrogen production apparatus further comprising a; unreacted gas separator for separating unreacted hydrocarbon gas contained in the hydrogen gas discharged from the heat exchange type carbon separator. 7. The method of claim 6,
Gas mixture installed on the hydrocarbon gas stream connecting the heat exchange type carbon separation unit and the reactor, and mixing the hydrocarbon gas discharged from the heat exchange type carbon separation unit and the unreacted hydrocarbon gas separated in the unreacted gas separator Hydrogen production apparatus comprising a part; According to claim 1,
The heat exchange type carbon separation unit, disposed in the outer flow path, hydrogen production apparatus, characterized in that it further comprises a flow guide member for promoting heat exchange between the mixed gas and the hydrocarbon gas. 9. The method of claim 8,
The flow guide member, Hydrogen production apparatus, characterized in that arranged in a spiral shape from a lower region of the outer passage through which hydrocarbon gas is introduced to an upper region of the outer passage through which hydrocarbon gas is discharged. 9. The method of claim 8,
The flow guide member, hydrogen production apparatus, characterized in that at least one of a hole, a groove and a protrusion is formed on the surface so as to promote convective heat exchange of the hydrocarbon gas moving along the outer flow path. 9. The method of claim 8,
The flow guide member is formed to extend from a lower region of the outer flow path through which hydrocarbon gas is introduced to an upper region of the outer flow path through which hydrocarbon gas is discharged, and maintain a uniform distance along the circumferential direction of the inner chamber. Hydrogen production device, characterized in that it is provided. 12. The method of claim 11,
The flow guide member,
an inner portion of a lower flow passage disposed in a lower region of the outer flow passage and extending obliquely to an upper side;
It is disposed in the upper region of the outer flow path, hydrogen production apparatus, characterized in that it comprises an upper flow inner portion extending vertically while going to the upper side.

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