System with raw material gas evaporation system and reforming system

Abstract

System, comprehensive: a raw material gas vaporization system (200) comprising a storage tank (210) for storing the raw material gas and a transmission line for transferring the raw material gas (10); a reforming system (100) comprising a reformer (120) for producing hydrogen (30) by reacting the raw material gas (10) with water, a burner (140) for applying heat to the reformer (120) and a pressure swing adsorption (PSA) system for separating the hydrogen in the mixed gas produced by the reformer (120); a CO2 separation device (300) for receiving exhaust gas in which the hydrogen (30) in the mixed gas has been removed by the PSA in order to remove carbon dioxide (CO2) by liquefying it through heat exchange with the transfer line of the raw material gas evaporation system (200), and a gas supply line (331) for supplying the remaining gas, wherein the CO2 has been removed in the CO2 separation device (300), to a burner as a fuel, characterized in that the reforming system (100) further comprises a boil-off gas (BOG) supply line (11) to which BOG generated by evaporation of the raw material gas stored in the storage tank (210) moves, and wherein the reformer (120) of the reforming system (100) generates hydrogen by reacting the BOG received from the BOG supply line (11) with water, using the BOG as the raw material gas.

Description

TECHNICAL BACKGROUND Technical field

[0001] The present disclosure relates to a system, and in particular a system for removing carbon dioxide from an exhaust gas stream generated by a reformer connected with a reforming system and a raw material gas evaporation system, thereby increasing the efficiency of the reformer. Description of the related technique

[0002] Hydrogen can be useful as an energy source or fuel because, apart from a very small amount of nitrogen oxide, it produces no environmentally hazardous byproducts, and it can be easily stored in various forms such as high-pressure gas, liquefied petroleum gas (LPG), and metal hydrides. Such technologies have been developed in various fields. One method for producing hydrogen is steam reforming, the most commercially available technology. This process uses natural gas, such as town gas, as a feedstock and can produce hydrogen through a reformer. Natural gas reforming is a technology for quickly and inexpensively converting gas into hydrogen fuel. Additional advantages of this process, which could be a key technology for the widespread adoption of fuel cells, include high efficiency, miniaturization, light weight, start-up stability, and speed.

[0003] Since steam reforming is a strongly endothermic reaction, the heat required for the reaction is supplied by burning a fuel gas in a burner to heat the reformer to a temperature of 750°C or more. Pressure swing adsorption (PSA) can be used to produce ultra-high purity hydrogen gas, which is then used to purify the hydrogen produced after the steam-methane reforming reaction. The exhaust gas from the PSA flows into the burner and is used together with the fuel gas for a heating reaction.

[0004] Meanwhile, in the case of a storage tank for raw material gases such as liquefied natural gas (hereinafter referred to as "LNG") and liquefied petroleum gas (hereinafter referred to as "LPG"), the raw material gases are continuously and naturally vaporized within the storage tank to produce boil-off gas (BOG). There is a risk of tank damage because pressure increases within the storage tank as the BOG accumulates, leading to varying treatment of the BOG produced. Different methods for treating the BOG have been disclosed, but the reliquefaction rate is limited, so if the amount of excess BOG is large, it is burned and consumed.

[0005] A common problem was burning the excess BOG to utilize its chemical energy, thus reducing energy efficiency and wasting energy. Furthermore, the exhaust gas from the PSA (presumably a specific product or system) contains carbon dioxide (CO2), increasing the energy required for combustion and consequently the required heat exchanger capacity.

[0006] The background described above is intended only to assist in understanding the background of the present disclosure and is not intended to suggest that the present disclosure falls within the field of related technology already known to the person skilled in the art.

[0007] Document JP 2003 81 605 A is known, which describes a process for producing hydrogen using LNG as a raw material to obtain pure hydrogen.

[0008] Furthermore, JP 2016 84 272 A is known. It describes a process for producing hydrogen gas that has a high purity. PRESENTATION OF REVELATION

[0009] The present invention aims to solve the problems mentioned above. One objective of the present disclosure is to provide a system that removes carbon dioxide (CO2) from exhaust gas by liquefying the carbon dioxide by connecting a reforming system with a raw material gas evaporation system, thereby improving the efficiency of a reformer, and to produce hydrogen by using evaporated gas, thereby improving fuel efficiency.

[0010] To achieve the objective, a system with the features according to claim 1 is provided. The system includes a BOG supply line to which boil-off gas (BOG) generated by evaporating the raw material gas stored in the storage tank moves, and the reformer of the reforming system can generate hydrogen by reacting the BOG received from the BOG supply line with water, using the BOG as the raw material gas.

[0011] The raw material gas evaporation system may also include an evaporation device for evaporating the raw material gas that has been heat-exchanged with the exhaust gas.

[0012] The CO2 separation device may include an exhaust gas compressor for compressing the exhaust gas emitted by the PSA, and the exhaust gas compressor may compress the exhaust gas to a pressure of 20 bar gauge pressure (barg) or more and 30 barg or less.

[0013] The CO2 separation device includes a raw material gas exhaust gas heat exchanger connected to the transmission line and an exhaust gas supply line of the raw material gas evaporation system to cool the exhaust gas using the cold heat of the raw material gas as a refrigerant.

[0014] The CO2 separation device can include a CO2 separator for separating the liquefied CO2 in the exhaust gas or a CO2 tank for storing the liquefied CO2.

[0015] Furthermore, if the exhaust gas exchanges heat with the raw material gas system, the temperature of the exhaust gas can be cooled to -40°C or less and -50°C or more.

[0016] The raw material gas vaporization system may include a BOG compressor for compressing the BOG from the storage tank, so that the high-pressure BOG flows into the BOG supply line. The system may further include a first pump connected to the storage tank for compressing and transferring the raw material gas, and a suction vessel for reliquefying a portion of the BOG by directing a portion of the BOG that has passed through the BOG compressor into the BOG supply line and mixing the remainder with the raw material gas transferred by the first pump. Furthermore, the first pump may compress the raw material gas to 1 barg or more and 10 barg or less.

[0017] Furthermore, the system can include a second pump connected to the intake tank to compress and transfer the raw material gas that has passed through the intake tank in order to exchange the high-pressure raw material gas with the exhaust gas for heat exchange, and the second pump can compress the raw material gas to 10 barg or more and 100 barg or less.

[0018] The reforming system may also include a water supply device for supplying water and several water heat exchangers for evaporation by applying heat to the water and supplying the evaporated water to the reformer.

[0019] The reforming system may also include a mixed-gas heat exchanger for cooling the mixed gas passing through the reformer by exchanging heat with a coolant. The reforming system may also be configured to include a transformer for producing hydrogen by reacting the CO generated in the reformer.

[0020] The present invention can reduce the CO2 emissions of the exhaust gas released from the reformer of the reforming system in order to remove the CO2 flowing into the burner, thereby reducing the waste of the heat required to warm the CO2. Furthermore, the excess BOG generated in the raw material gas vaporization system can be used to produce hydrogen instead of being burned and consumed, thus improving fuel efficiency and increasing economic viability. SHORT FIGURE DESCRIPTION

[0021] The above and other aims, features and other advantages of the present invention will be more clearly understood by the following detailed description when considered in conjunction with the accompanying drawings, which: Fig. 1 is a block diagram of a reforming system. Fig. Figure 2 is a block diagram of a raw material gas vaporization system. Fig. Figure 3 is a block diagram of a reforming system connected to the raw material gas evaporation system according to an embodiment of the present disclosure. Fig. Figure 4 is a block diagram of a carbon dioxide (CO2) separation device of the reforming system connected with the raw material gas evaporation system according to an embodiment of the present disclosure. Fig. Figure 5 is a graph representing an exemplary liquefiable rate of CO2 according to an environmental condition of the CO2 separation device of the reforming system connected with the raw material gas evaporation system according to an embodiment of the present disclosure. Fig. Figure 6 is a graph showing an exemplary efficiency of a reforming system according to the ambient conditions of the CO2 separation device of the reforming system connected to the raw material gas evaporation system according to an embodiment of the present disclosure. DETAILED DESCRIPTION OF THE REVELATION

[0022] Specific structural and functional descriptions of the embodiments disclosed in this specification or application are provided solely for the purpose of describing the embodiments according to this disclosure. The embodiments according to this disclosure can be implemented in different forms and it should not be interpreted as being limited to the embodiments described in this description or application.

[0023] Since the embodiments according to the present disclosure can be modified in various ways and can have different forms, particular embodiments are illustrated in the drawings and described in detail in the present specification or application. However, this is not intended to limit the embodiments according to the concept of the present disclosure to the embodiments according to a specific disclosed form. It should be understood as including all modifications, equivalents, and substitutions contained in the basic idea and scope of the present disclosure.

[0024] Terms such as first and / or second may be used to describe different components; however, the components are not intended to be limited by these terms. The terms are used only for the purpose of distinguishing one component from another. For example, the first component may be referred to as a second component without deviating from the scope as defined in the present disclosure, and similarly, the second component may be referred to as the first component.

[0025] In the following, embodiments of the present disclosure will be described with reference to the accompanying drawings in order to describe the present disclosure in detail. The same reference numerals shown in the drawings denote the same elements. Different components, i.e., devices, units, elements, and the like of the present disclosure, may be described herein as having a particular purpose or performing a particular function, process, and the like. Such components may be said to be "designed" to achieve or fulfill the particular purpose, or to perform, complete, execute, generate, or the like the particular function, process, and the like.

[0026] The present disclosure relates to a reforming system 100 connected to a raw material gas vaporization system. The reforming system 100 serves to produce hydrogen using boil-off gas (BOG) by connecting a raw material gas vaporization system 200 to the reforming system 100. The reforming system 100 thereby improves economic efficiency and, by removing carbon dioxide (CO2) from the exhaust gas, improves the efficiency of the reforming system 100.

[0027] Fig. Figure 1 is a block diagram of the Reform System 100. The general Reform System 100 is briefly described below with reference to Fig. 1. will be described.

[0028] With reference to Fig. The reforming system 100 can comprise a raw material gas 10, a raw material gas compressor 110, a reformer 120, a transformer 180, water 20, a water supply device 150, one or more heat exchangers 161, 162, 163, 164, and a pressure swing absorption chiller (PSA) 130. The raw material gas can be composed of different raw material gases that are transferred in a liquefied state and vaporized, such as LPG and LNG.

[0029] The reforming system 100 is a system for producing hydrogen 30 by reacting the raw material gas 10 with the water 20. A chemical reaction in the reformer 120, in which a reforming reaction takes place, was as follows, where CH4 is methane, H2O is water, CO is carbon monoxide and 3H2 represents three hydrogen molecules. CH4 + H2O → CO + 3H2

[0030] A methane vapor reforming reaction is a strongly endothermic reaction. Therefore, since the forward reaction proceeds actively under high-temperature conditions, the reforming system 100 is designed to include a burner 140 for supplying heat of reaction to the reformer 120. The conventional reforming system combusts the raw material gas 10, such as town gas and / or exhaust gas emitted by the PSA 130, as a fuel in the burner 140 to supply the heat of reaction to the reformer 120. Furthermore, the raw material gas 10 can be the boil-off gas (BOG) produced by vaporizing the raw material gas 10, which is in a liquid state.

[0031] Reforming system 100 generates carbon monoxide along with hydrogen 30 during the reforming of hydrocarbons. Since carbon monoxide acts as a catalyst poison in an electrode of a fuel cell stack, it can be removed. The carbon monoxide removal reaction can utilize a shift reaction, such as the following formula, where H2 represents a single hydrogen molecule. CO + H2O → CO2 + H2

[0032] Since the ordinary reforming system 100 is a design for combustion by supplying exhaust gas to the burner 140, and since the carbon dioxide contained in the exhaust gas was to be heated together, there was a problem of heat waste, and there was a problem in that carbon dioxide is contained in the exhaust gas, which increases the required heat capacity of a heat exchanger.

[0033] Fig. Figure 2 is a block diagram of the raw material gas vaporization system 200. The general raw material gas vaporization system 200 is briefly described with reference to Fig. 2 can be described as follows.

[0034] The raw material gas vaporization system 200 is a system for pressurizing and vaporizing raw material gas 10, such as cryogenic LNG at -160°C or less, in order to supply the gas 10 to a demand source 270 that requires energy. The raw material gas vaporization system 200 can include a storage tank 210, a first pump 221, a suction tank 240, a second pump 222, a vaporization device 250, a BOG compressor 230, and a BOG reliquefaction device 260. The system 200 can process the BOG generated in the storage tank 210.

[0035] Even if storage tank 210 is thermally insulated, external heat can be continuously supplied to storage tank 210. Thus, the raw material gas 10 is continuously and naturally vaporized in storage tank 210, thereby generating the BOG in storage tank 210.

[0036] If the BOG accumulates in storage tank 210, there is a risk of damage to the tank because the pressure in storage tank 210 increases, causing the BOG generated in storage tank 210 to be processed differently. For example, the BOG can be reliquefied by the reliquefaction device 260 to recover the BOG from storage tank 210. In another example, the BOG can be reliquefied by mixing it with the raw material gas 10 transferred at high pressure through the intake hopper 240. In yet another example, the BOG can be consumed in a self-generator 280 using the BOG as a fuel for power generation. If the amount of excess BOG is large, it can be burned and consumed in a combustion device 290.

[0037] One problem was that burning and consuming the excess BOG consumed the chemical energy contained within it. There was also a problem of environmental pollution due to the large amount of CO2 produced during the combustion process.

[0038] Fig. Figure 3 is a block diagram of the reforming system connected to the raw material gas evaporation system according to an embodiment of the present disclosure.

[0039] With reference to Fig. Figure 3 shows a reforming system connected to the raw material gas evaporation system according to an embodiment of the present disclosure. The reforming system of Fig. 3 may comprise: The raw material gas evaporation system 200, comprising the storage tank 210 for storing the raw material gas 10 and a transmission line for transferring the raw material gas 10; the reforming system, comprising a reformer 120 for producing the hydrogen 30 by reacting the raw material gas 10 with the water 20, the burner 140 for supplying heat to the reformer 120 and the PSA 130 for separating the hydrogen 30 in the mixed gas produced by the reformer 120; the CO2 separation device 300 for removing CO2 by liquefaction by receiving the exhaust gas in which the hydrogen in the mixed gas has been removed by the PSA 130, in order to exchange heat with the transmission line of the raw material gas evaporation system 200; and a gas supply line 331 for supplying the remaining gas, wherein CO2 has been removed in the CO2 separation device, to a burner as a fuel.

[0040] The raw material gas evaporation system according to one embodiment of the present disclosure can remove CO2 from the exhaust gas generated in the reforming system by liquefying it via a heat exchanger connected to the raw material gas evaporation system. The raw material gas evaporation system can include the CO2 separation device 300 for heat exchange with the raw material gas evaporation system in order to liquefy the CO2 contained in the exhaust gas before combustion by feeding the exhaust gas discharged by the PSA 130 to the burner 140.

[0041] Since the raw material gas 10 is in a cryogenic liquid state in the raw material gas vaporization system until it is vaporized, CO2 can be liquefied. For this purpose, the CO2 separation device 300 can be designed to connect the exhaust gas emitted by the PSA 130 with the raw material gas vaporization system 200.

[0042] Furthermore, the reforming system connected to the raw material gas evaporation system according to an embodiment of the present disclosure can also include a BOG supply line 11 to which the BOG generated by evaporating the raw material gas 10 stored in the storage tank 210 flows. The reformer 120 of the reforming system can be configured to generate the hydrogen 30 by reacting the BOG received from the BOG supply line 11 with the water 20, using the BOG as the raw material gas 10.

[0043] As described above, since the BOG is produced by vaporizing the raw material gas 10 and is made from hydrocarbons, the hydrogen 30 can be generated by supplying the raw material gas 10 to the reforming system. The BOG generated in the storage tank 210 flows through the BOG supply line 11 into the reforming system. The hydrogen 30 can be generated by reforming the received BOG, thereby improving fuel efficiency.

[0044] The raw material gas vaporization system can further include the BOG compressor 230 for compressing the BOG, so that the pressurized (e.g., high-pressure) BOG flows into the BOG supply line 11. The BOG compressor 230 can compress the BOG to 1 barg or more and 10 barg or less.

[0045] Furthermore, the raw material gas vaporization system can include a first pump 221 connected to the storage tank 210 for compressing and transferring the raw material gas 10, and an intake vessel 240 for reliquefying a portion of the BOG by directing the portion of the BOG that has passed through the BOG compressor 230 into the BOG supply line 11, and mixing the remainder with the raw material gas 10 transferred by the first pump 221. The intake vessel 240 can reliquefy the BOG by mixing it with the raw material gas 10, thereby increasing fuel efficiency. The first pump can compress the raw material gas 10 to 1 barg or more and 10 barg or less.

[0046] Furthermore, the raw material gas vaporization system 200 can also include a second pump 222 connected to the intake vessel 240 to compress and transfer the raw material gas 10 that has passed through the intake vessel 240, in order to compress the raw material gas 10 to a high pressure. The second pump can compress the raw material gas 10 to 10 barg or more and 100 barg or less.

[0047] Furthermore, the raw material gas vaporization system 200 may also include a vaporization device 250 for vaporizing the raw material gas 10 after heat exchange with the exhaust gas. The vaporization device 250 may be one of a variety of vaporization devices 250 used in LNG vaporization. The vaporization device 250 may include a general open-rack vaporizer (ORV), a submerged combustor, or the like.

[0048] The reforming system can include the water supply device 150 for supplying the water 20 and one or more of the several water heat exchangers 161, 162, 163, 164 for evaporating the water by heating and for supplying the evaporated water to the reformer 120. The water 20 required for the reforming reaction can be pure water or ultrapure water.

[0049] Furthermore, the reforming system 100 can be designed to include a mixed-gas heat exchanger 170 for cooling the gas passing through the reformer 120 by heat exchange with a coolant. The mixed-gas heat exchanger 170 can reduce the temperature of the mixed gas heated in the reforming process. The size of the mixed-gas heat exchanger 170 is determined according to the quantity of mixed gas discharged from the reformer 120. For example, if the quantity of mixed gas is reduced, the size of the mixed-gas heat exchanger 170 can also be reduced.

[0050] Furthermore, the reforming system 100 can be configured to include the transformer 180 for generating hydrogen 30 by reacting the CO produced in the reformer 120. The transformer 180 is a device for generating hydrogen 30, for example, by reacting the CO with the water 20, as in the reaction formula described above, and can generate the hydrogen 30 by removing the CO.

[0051] Fig. Figure 4 is a block diagram of the CO2 separation device 300 of the reforming system 100 connected with the raw material gas evaporation system according to an embodiment of the present disclosure. Fig. Figure 5 is a graph representing a liquefiable rate of CO2 according to the ambient conditions of the CO2 separation device of the reforming system associated with the raw material gas evaporation system according to an embodiment of the present disclosure. Fig. Figure 6 is a graph representing the efficiency of the reforming system according to the environmental conditions of the CO2 separation device of the reforming system connected with the raw material gas evaporation system according to the embodiment of the present disclosure.

[0052] The CO2 separation device 300 is described in detail with reference to Fig. 4-6 are described as follows.

[0053] The CO2 separation device 300 can include an exhaust gas compressor 310, a raw material gas and exhaust gas heat exchanger 320, a CO2 separator 330 and a CO2 tank 340.

[0054] Since CO2 sublimates without passing through the liquid state when cooled at the triple point pressure or below, liquefaction can be carried out at the triple point pressure and temperature or higher. The triple point pressure of CO2 is 4.2 barg and its temperature is -57°C. Therefore, the pressure of the CO2 in the CO2 separation device 300 can be 4.2 barg or higher, and the temperature can be -57°C or higher.

[0055] The exhaust compressor 310 is a device for compressing the exhaust gas emitted by the PSA 130 to a high pressure. The exhaust compressor 310 can be connected to the PSA 130 to receive the exhaust gas.

[0056] Fig. 5 and Fig. Figure 6 represents the liquefiable rate of CO2 and the efficiency of the reformer system according to the pressure that compressed the exhaust gas in the exhaust gas compressor 310. Each graph shows the liquefiable rate of CO2 and the efficiency of the reformer system when compressed at 50 barg (data series 400); 40 barg (data series 500); 30 barg (data series 600); 20 barg (data series 700); and 10 barg (data series 800).

[0057] With reference to Fig. 5. It can be confirmed that when the pressure of the exhaust gas compressed by the exhaust compressor 310 increases, the liquefiable rate of CO2 also increases. The ratio increases as the difference with the triple point pressure of CO2 increases with the pressure increase, thereby increasing the liquefiable temperature range.

[0058] With reference to Fig. 6. It can be confirmed that if the exhaust gas pressure exceeds a certain pressure, the efficiency of the reforming system is reduced. As in Fig. As shown in Figure 6, at -40°C the efficiency of the reforming system at 50 barg (400) appears lower than the efficiency at 30 barg (600) and at 20 barg (700). This is due to the Joule-Thomson effect, in which the exhaust gas, compressed at high pressure, expands isentropically when it passes through a small hole as it is injected into the burner 140 via the gas supply line 311, thus reducing the temperature of the CO2. Therefore, the pressure of the exhaust gas after compression can be determined based on the liquefiable rate of CO2 and the efficiency of the reforming system. For example, a pressure of 20 barg or more and 30 barg or less can be determined.

[0059] The raw material gas exhaust gas heat exchanger 320 exchanges heat between the cryogenic raw material gas 10 and the exhaust gas. The raw material gas exhaust gas heat exchanger 320 can be connected to the transfer line and the exhaust gas feed line of the raw material gas evaporation system. Therefore, heat is exchanged between the raw material gas 10 of the raw material gas evaporation system and the exhaust gas of the CO2 separation device 300. The CO2 can be liquefied by cooling the exhaust gas using the heat of the raw material gas 10 as a refrigerant.

[0060] With reference to Fig. 5 and Fig. 6. When the exhaust gas exchanges heat with the raw material gas evaporation system, the liquefiable rate of CO2 and the efficiency of the reformer are higher the lower the cooling temperature of the exhaust gas. However, with reference to Fig. 6. If the exhaust gas cooling temperature is at or below a certain threshold temperature, the efficiency of the reforming system will decrease. Therefore, the exhaust gas should be cooled at a suitable temperature based on the liquefiable rate of CO2 and the efficiency of the reforming system. For example, the exhaust gas cooling temperature can be -40°C or less and -50°C or more.

[0061] Consequently, when considering the liquefiable rate of CO2 and the efficiency of the reforming system with reference to Fig. 5 and Fig. 6 Operating conditions of the CO2 separation device 300 are determined in an example as a pressure of 20 barg or more and 30 barg or less and a cooling temperature of -40°C or less or -50°C or more.

[0062] The CO2 separator 330 is a device for separating the liquefied CO2 after the exhaust gas exchanges heat with the raw material gas evaporation system to liquefy the CO2. The CO2 tank 340 is a device for storing the CO2 liquefied in the exhaust gas. The CO2 separated and liquefied in the exhaust gas can advantageously be handled separately by the CO2 separator 330 and the CO2 tank 340.

[0063] The raw material gas vaporization system according to one embodiment of the present disclosure can remove CO2 from the exhaust gas, thereby reducing the CO2 emission of the reformer 120. For example, the CO2 emission of the reformer 120 can be reduced by 45%. Furthermore, since the amount of exhaust gas from the burner 140 is reduced by removing the CO2, the size of the mixed gas heat exchanger 170 can be reduced. For example, the size of the mixed gas heat exchanger 170 can be reduced by 9%. Furthermore, the excess BOG can be used to generate hydrogen 30 without combustion and consumption, thereby increasing fuel efficiency.

[0064] While the present disclosure has presented and described certain embodiments, it should be apparent to the person skilled in the art that the present disclosure can be improved and modified in various ways without deviating from the basic technical concept of the technical disclosure provided by the following claims.

Claims

[1] System, encompassing: a raw material gas vaporization system (200) comprising a storage tank (210) for storing the raw material gas and a transmission line for transferring the raw material gas (10); a reforming system (100) comprising a reformer (120) for producing hydrogen (30) by reacting the raw material gas (10) with water, a burner (140) for applying heat to the reformer (120) and a pressure swing adsorption (PSA) system for separating the hydrogen in the mixed gas produced by the reformer (120); a CO2 separation device (300) for receiving exhaust gas in which the hydrogen (30) in the mixed gas has been removed by the PSA in order to remove carbon dioxide (CO2) by liquefying it through heat exchange with the transfer line of the raw material gas evaporation system (200), and a gas supply line (331) for supplying the remaining gas, wherein the CO2 has been removed in the CO2 separation device (300), to a burner as a fuel, characterized by , that the reforming system (100) further comprises a boil-off gas (BOG) supply line (11) to which BOG generated by evaporation of the raw material gas stored in the storage tank (210) moves, and wherein the reformer (120) of the reforming system (100) generates hydrogen by reacting the BOG received from the BOG supply line (11) with water, using the BOG as the raw material gas. [2] System according to one of the preceding claims, wherein the raw material gas evaporation system (200) further comprises an evaporation device (250) for evaporating the raw material gas which has been heat-exchanged with the exhaust gas. [3] System according to one of the preceding claims, wherein the CO2 separation device (300) comprises an exhaust gas compressor (310) for compressing the exhaust gas emitted by the PSA. [4] System according to claim 3, wherein the exhaust gas compressor (310) compresses the exhaust gas pressure to 20 barg or more and 30 barg or less. [5] System according to one of the preceding claims, wherein the CO2 separation device (300) comprises a raw material gas exhaust gas heat exchanger (320) connected to the transmission line and an exhaust gas supply line of the raw material gas evaporation system (200) to cool the exhaust gas using the cold heat of the raw material gas as a refrigerant. [6] System according to one of the preceding claims, wherein the CO2 separation device (300) comprises a CO2 separator (330) for separating the CO2 liquefied in the exhaust gas. [7] System according to one of the preceding claims, wherein the CO2 separation device (300) has a CO2 tank (340) for storing the liquefied CO2. [8] System according to any of the preceding claims, wherein when the exhaust gas exchanges heat with the raw material gas system, the temperature of the exhaust gas is cooled to -40°C or less and -50°C or more. [9] System according to one of the preceding claims, wherein the raw material gas evaporation system (200) further comprises a BOG compressor (230) for compressing the BOG of the storage tank (210) so that the high-pressure BOG flows into the BOG supply line (11). [10] System according to claim 9, wherein the raw material gas evaporation system (200) further comprises a first pump (221) connected to the storage tank (210) for compressing and transferring the raw material gas (10), and an intake vessel (240) for reliquefying a portion of the BOG by directing the portion of the BOG that has passed through the BOG compressor (230) into the BOG supply line (11) and mixing the remainder with the raw material gas transferred by the first pump. [11] System according to claim 10, wherein the first pump (221) compresses the raw material gas to 1 barg or more and 10 barg or less. [12] System according to claim 10 or 11, further comprising a second pump (222) connected to the intake container (240) to compress and transfer the raw material gas (10) that has passed through the intake container (240) in order to exchange the high-pressure raw material gas (10) with the exhaust gas for heat exchange. [13] System according to claim 12, wherein the second pump (222) compresses the raw material gas (10) to 10 barg or more and 100 barg or less. [14] System according to one of the preceding claims, wherein the reforming system (100) further comprises a water supply device (150) for supplying water and several water heat exchangers (161, 162, 163, 164) for evaporation by applying heat to the water and supplying the evaporated water to the reformer (120). [15] System according to one of the preceding claims, wherein the reforming system (100) further comprises a mixed gas heat exchanger (170) for cooling the mixed gas passed through the reformer (120) by heat exchange with a coolant. [16] System according to one of the preceding claims, wherein the reforming system (100) further comprises a transformer (180) for producing hydrogen by reacting the CO produced in the reformer (120).

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