阅读说明：本技术 与原料气体汽化系统连接的重整系统 (Reforming system connected to raw gas vaporization system ) 是由 高东石 于 2020-06-10 设计创作，主要内容包括：本申请涉及一种与原料气体汽化系统连接的重整系统,包括：原料气体汽化系统,包括储存原料气体的储罐和输送原料气体的输送管路；重整系统,包括通过使原料气体与水反应来产生氢的重整器、向重整器供应热的燃烧器、以及从重整器产生的混合气体中分离氢的变压吸附(PSA)；CO-2分离装置,从PSA接收已去除混合气体中的氢的废气,并通过与原料气体汽化系统的输送管路的热交换使CO-2液化来去除CO-2；以及气体供应管路,将CO-2分离装置中已去除CO-2的残留气体作为燃料供应到燃烧器。(The present application relates to a reforming system connected to a raw gas vaporization system, comprising: the raw material gas vaporization system comprises a storage tank for storing the raw material gas and a conveying pipeline for conveying the raw material gas; a reforming system comprising a reformer for generating hydrogen by reacting a raw material gas with water, a burner for supplying heat to the reformer, and a fuel cell system produced from the reformerPressure Swing Adsorption (PSA) for separating hydrogen from the raw mixed gas; CO2 2 A separation device for receiving the waste gas from which hydrogen in the mixed gas has been removed from the PSA and for causing CO to exchange heat with the transfer line of the raw material gas vaporization system 2 Liquefaction to remove CO 2 (ii) a And a gas supply line for supplying CO 2 CO removal in the separation unit 2 Is supplied as fuel to the burner.)

1. A reforming system coupled to a feed gas vaporization system, comprising:

the raw material gas vaporization system comprises a storage tank for storing the raw material gas and a conveying pipeline for conveying the raw material gas;

a reforming system including a reformer that generates hydrogen by reacting the raw gas with water, a combustor that supplies heat to the reformer, and a Pressure Swing Adsorption (PSA) that separates the hydrogen from a mixed gas generated by the reformer;

CO₂a separation device that receives the off-gas from which the hydrogen in the mixed gas has been removed from the PSA, and causes CO to be exchanged by heat with the transfer line of the raw material gas vaporization system₂Liquefaction to remove CO₂(ii) a And

a gas supply line for supplying the CO₂The CO is removed in a separation unit₂Is supplied as fuel to the burner.

2. The reforming system of claim 1,

the reforming system further includes a boil-off gas supply line through which the BOG generated by vaporizing the raw material gas stored in the storage tank moves, and

the reformer of the reforming system generates hydrogen by reacting the BOG received from the BOG supply line as the raw material gas with water.

3. The reforming system of claim 1,

the raw material gas vaporization system further includes a vaporization device that vaporizes the raw material gas that exchanges heat with the off-gas.

4. The reforming system of claim 1,

the CO is₂The separation device includes a waste gas compressor that compresses the waste gas discharged from the PSA.

5. The reforming system of claim 4,

the off-gas compressor compresses the pressure of the off-gas to above 20barg and below 30 barg.

6. The reforming system of claim 1,

the CO is₂The separation device includes a raw gas and off gas heat exchanger connected to the transfer line and off gas supply line of the raw gas vaporization system to cool the off gas using cold heat of the raw gas as a refrigerant.

7. The reforming system of claim 1,

the CO is₂The separation device comprises a separator for separating CO liquefied in the exhaust gas₂CO of₂A separator.

8. The reforming system of claim 1,

the CO is₂The separation unit comprises storage of said liquefied CO₂CO of₂And (7) a tank.

9. The reforming system of claim 1,

the temperature of the exhaust gas is cooled to below-40 ℃ and above-50 ℃ when the exhaust gas is heat exchanged with the feed gas system.

10. The reforming system of claim 1,

the feed gas vaporization system further includes a BOG compressor that compresses the BOG of the storage tank to flow high pressure BOG into a BOG supply line.

11. The reforming system of claim 10,

the raw material gas vaporization system further includes: a first pump connected to the storage tank to compress and transfer the raw material gas; and a suction drum, a part of the BOG passing through the BOG compressor flows into the BOG supply line, and the remaining BOG is mixed with the raw material gas delivered by the first pump, so that a part of the BOG is reliquefied.

12. The reforming system of claim 11,

the first pump compresses the feed gas to above 1barg and below 10 barg.

13. The reforming system of claim 11, further comprising:

a second pump connected to the suction drum to compress and transfer the raw gas passing through the suction drum, thereby heat-exchanging high-pressure raw gas with the offgas.

14. The reforming system of claim 13,

the second pump compresses the feed gas to above 10barg and below 100 barg.

15. The reforming system of claim 1,

the reforming system further comprises: a water supply device for supplying water; and a plurality of water heat exchangers vaporizing water by applying heat to the water and supplying the vaporized water to the reformer.

16. The reforming system of claim 1,

the reforming system further includes a mixed gas heat exchanger that cools by heat-exchanging the mixed gas passing through the reformer with a coolant.

17. The reforming system of claim 1,

the reforming system further includes a shift converter that generates hydrogen by reacting CO generated in the reformer.

Technical Field

The present disclosure relates to a reforming (reforming) system, and more particularly, to a reforming system that improves the efficiency of a reformer by connecting a reforming system and a raw gas vaporization system to remove carbon dioxide from an exhaust gas generated in the reformer.

Background

When hydrogen is used as a fuel, there are no products harmful to the environment except for a very small amount of nitrogen oxides, and hydrogen can be easily stored in various forms, for example, in the form of high-pressure gas, liquid gas, and metal hydride, and thus, technologies for using hydrogen as an energy source are being developed in various fields. The hydrogen production method is the most commercialized technology of steam reforming, and hydrogen can be produced by using natural gas such as town gas as a raw material and passing through a reformer. Natural gas reforming is a technology for rapidly and economically converting natural gas into hydrogen fuel. The method can be said to be a core technology for popularizing the fuel cell, and has the advantages of high efficiency, miniaturization, light weight, stable and quick start and the like.

Since the steam reforming reaction is a strong endothermic reaction, the reformer is heated to a temperature above 750 ℃ by burning the fuel gas in a burner to supply the heat required for the reaction. The hydrogen in the gas produced after the steam-methane reforming reaction can be purified by Pressure Swing Adsorption (PSA) to produce ultra-high purity hydrogen. The waste gas of the PSA flows into the burner and is used together with the fuel gas for heating the reaction.

Meanwhile, in the case of a storage tank storing a raw material Gas such as Liquefied Natural Gas (hereinafter, referred to as "LNG") and Liquefied Petroleum Gas (hereinafter, referred to as "LPG"), the raw material Gas is continuously and naturally vaporized in the storage tank, thereby generating Boil-Off Gas (BOG) within the storage tank. Since the pressure of the storage tank rises when the BOG accumulates in the storage tank, there is a risk of damage to the storage tank, and thus, various processes are performed on the BOG generated in the storage tank. Various methods of handling BOG have been disclosed, but the reliquefiability is limited so that when the amount of excess BOG is large, BOG is consumed by burning it.

In the prior art, excessive BOG is combusted, so that chemical energy of BOG is consumed by combustion, and thus there are problems that energy efficiency is reduced and energy is wasted. The PSA waste gas includes carbon dioxide (CO)₂) Therefore, there is a problem in that the energy required for combustion increases and the required capacity size of the heat exchanger increases.

The foregoing explained as background is intended only to aid in understanding the background of the present disclosure and is not intended to represent that the present disclosure falls within the scope of the related art known to those skilled in the art.

Disclosure of Invention

The present disclosure is directed to solving the above problems. An object of the present disclosure is to provide a reforming system that can vaporize carbon dioxide (CO) by connecting the reforming system with a raw material gas vaporization system₂) The liquefaction removes carbon dioxide in the exhaust gas to improve the efficiency of the reformer, and generates hydrogen by using the vaporized gas to improve fuel efficiency.

To achieve the object, the reforming system of the present disclosure connected to the raw material gas vaporization system may include: the raw material gas vaporization system comprises a storage tank for storing the raw material gas and a conveying pipeline for conveying the raw material gas; a reforming system including a reformer that generates hydrogen by reacting a raw material gas with water, a combustor that supplies heat to the reformer, and Pressure Swing Adsorption (PSA) that separates hydrogen from a mixed gas generated by the reformer; CO2₂A separation device for receiving the waste gas from which hydrogen in the mixed gas has been removed from the PSA and for causing CO to exchange heat with the transfer line of the raw material gas vaporization system₂Liquefaction to remove CO₂(ii) a And a gas supply line to be connected to CO₂CO removal in the separation unit₂Is supplied as fuel to the burner.

The reforming system may further include a BOG supply line through which a boil-off gas (BOG) generated by vaporizing the raw material gas stored in the storage tank is moved, and the reformer of the reforming system may generate hydrogen by reacting the BOG received from the BOG supply line with water as the raw material gas.

The raw material gas vaporization system may further include a vaporization device that vaporizes the raw material gas that exchanges heat with the off-gas.

The CO2 separation device may include a waste gas compressor for compressing waste gas discharged from the PSA, and the waste gas compressor may compress the pressure of the waste gas to above 20barg (bar gauge pressure) and below 30 barg.

In addition, CO₂The separation device may include a raw gas and off gas heat exchanger connected to the transfer line and the off gas supply line of the raw gas vaporization system to cool the off gas using the cold heat of the raw gas as a refrigerant.

In addition, CO₂The separation device may comprise separation of liquefied CO in the exhaust gas₂CO of₂Separator and storage of liquefied CO₂CO of₂And (7) a tank.

Further, the temperature of the exhaust gas may be cooled to below-40 ℃ and above-50 ℃ when the exhaust gas is heat exchanged with the feed gas system.

The feed gas vaporization system may include a BOG compressor that compresses the BOG of the storage tank to flow high pressure BOG into the BOG supply line. The raw material gas vaporization system may further include: a first pump connected to the storage tank to compress and transfer the raw material gas; and a suction drum for re-liquefying a part of the BOG supplied from the BOG compressor by flowing a part of the BOG into the BOG supply line and mixing the remaining BOG with the raw gas supplied from the first pump. Further, the first pump may compress the raw material gas to 1barg or more and 10barg or less.

Further, the reforming system connected to the raw material gas vaporization system may include a second pump connected to the suction drum to compress and convey the raw material gas passing through the suction drum so as to heat-exchange the high-pressure raw material gas with the off-gas, and the second pump may compress the raw material gas to 10barg or more and 100barg or less.

The reforming system may further comprise: a water supply device for supplying water; and a plurality of water heat exchangers vaporizing water by applying heat to the water and supplying the vaporized water to the reformer.

The reforming system may further include a mixed gas heat exchanger that performs cooling by heat-exchanging the mixed gas passing through the reformer with a coolant. The reforming system may be configured to further include a shift converter that generates hydrogen by reacting CO generated in the reformer.

The present disclosure may reduce CO in exhaust gas discharged from a reformer of a reforming system₂Emission of CO to remove CO flowing into the combustor₂Thereby reducing heating CO₂The waste of heat required. In addition, the excess BOG generated in the raw gas vaporization system may be used to generate hydrogen rather than being consumed by combustion, thereby improving fuel efficiency to improve economy.

Drawings

The above and other objects, features and other advantages of the present disclosure will be more clearly understood from the following detailed description taken in conjunction with the accompanying drawings, in which:

FIG. 1 is a block diagram of a reforming system.

Fig. 2 is a block diagram of a raw material gas vaporization system.

FIG. 3 is a block diagram of a reforming system coupled to a feed gas vaporization system according to an embodiment of the present disclosure.

FIG. 4 is a carbon dioxide (CO) of a reforming system coupled to a raw gas vaporization system according to an embodiment of the present disclosure₂) Block diagram of a separation device.

FIG. 5 is a diagram showing CO based reforming system coupled to a raw gas vaporization system according to an embodiment of the present disclosure₂Separation of ambient CO of plant₂Graph of the liquefaction rate of (a).

FIG. 6 is a diagram showing CO based reforming system coupled to a raw gas vaporization system according to an embodiment of the present disclosure₂Graph of example efficiencies of reformer systems for ambient conditions of the separation device.

Detailed Description

The specific structural and functional descriptions of the embodiments of the present disclosure disclosed in this specification or application are presented solely for the purpose of describing embodiments in accordance with the present disclosure. Embodiments in accordance with the present disclosure may be embodied in various forms and should not be construed as limited to the embodiments set forth in this specification or application.

While embodiments in accordance with the present disclosure are susceptible to various modifications and alternative forms, specific embodiments have been shown in the drawings and are described in detail in this specification or application. However, it is not intended to limit embodiments of concepts according to the present disclosure to the particular forms disclosed. And all changes, equivalents, and alternatives falling within the spirit and scope of the disclosure are intended to be embraced thereby.

Terms such as first and/or second may be used to describe various components, but these components should not be limited by the terms. The terminology is used only for the purpose of distinguishing one component from another. For example, a first component may be termed a second component, and, similarly, a second component may be termed a first component, without departing from the scope of concepts according to the present disclosure.

Hereinafter, embodiments of the present disclosure are described with reference to the accompanying drawings to describe the present disclosure in detail. Like reference numerals in the drawings denote like elements. Various components of the present disclosure, i.e., devices, units, elements, may be described herein as having a particular purpose or performing a particular function, process, etc. Such components may be referred to as being "configured to" achieve or satisfy a particular purpose, or to perform, complete, perform, or produce a particular function, process, or the like.

The present disclosure relates to a reforming system 100 coupled to a raw gas vaporization system. Hydrogen is generated by connecting the raw gas vaporization system 200 with the reforming system 100 to use boil-off gas (BOG). The reforming system 100 thus improves economy and removes carbon dioxide (CO) from the exhaust gas₂) To increase the efficiency of the reforming system 100.

Fig. 1 is a block diagram of a reforming system 100. A conventional reforming system 100 is briefly described below with reference to fig. 1.

Referring to fig. 1, a reforming system 100 may include a raw gas 10, a raw gas compressor 110, a reformer 120, an inverter 180, water 20, a water supply device 150, a plurality of heat exchangers 161 to 164, and a Pressure Swing Adsorption (PSA) 130. The feed gas may include various feed gases, such as LNG and LPG, which are transported and vaporized in a liquefied state.

The reforming system 100 is a system that generates hydrogen 30 by reacting a raw material gas 10 with water 20. The chemical reaction in the reformer 120 generating the reforming reaction is as follows.

CH₄+H₂O→CO+3H₂

Wherein, CH₄Is methane, H₂O is water, CO is carbon monoxide, 3H₂Three hydrogen molecules are indicated.

The methane-steam reforming reaction is a strongly endothermic reaction. Since the positive reaction is actively generated under the high temperature condition, the reforming system 100 is configured to include a combustor 140 for supplying reaction heat to the reformer 120. The conventional reforming system 100 burns a raw material gas 10 such as a town gas and/or an exhaust gas discharged from the PSA130 as a fuel in the combustor 140 to supply reaction heat to the reformer 120. Further, the raw material gas 10 may be BOG generated by vaporizing the raw material gas 10 in a liquid state.

In the reforming system 100, carbon monoxide is produced along with hydrogen as the hydrocarbons are reformed. Since carbon monoxide acts as a catalyst poison on a catalyst used in an electrode of a fuel cell stack, a process for removing carbon monoxide is required. In general, the reaction of removing carbon monoxide may utilize a shift reaction such as the following reaction formula.

CO+H₂O→CO₂+H₂

Wherein H₂Represents a single hydrogen molecule.

Since the conventional reforming system 100 is configured to perform combustion by supplying exhaust gas to the combustor 140, and since carbon dioxide included in the exhaust gas needs to be heated together, there are problems in that heat is wasted, and there is a problem in that the heat capacity of the heat exchanger required due to the inclusion of carbon dioxide in the exhaust gas increases.

Fig. 2 is a block diagram of a feed gas vaporization system 200. A conventional raw material gas vaporization system 200 is briefly described below with reference to fig. 2.

The raw material gas vaporization system 200 is a system for compressing the raw material gas 10 (for example, LNG having an extremely low temperature of-160 ℃ or lower) and vaporizing the raw material gas 10 to supply the vaporized raw material gas to the energy source 270. The raw gas vaporization system 200 may include a storage tank 210, a first pump 221, a suction drum 240, a second pump 222, and a vaporization apparatus 250, and may include a BOG compressor 230 and a BOG reliquefaction apparatus 260 to process the BOG generated in the storage tank 210.

Although the storage tank 210 may be insulated, external heat may be continuously transferred to the storage tank 210. Accordingly, the raw material gas 10 is continuously and naturally vaporized in the storage tank 210, thereby generating BOG in the storage tank 210.

When the BOG is accumulated in the storage tank 210, since the pressure of the storage tank 210 is increased, there is a risk of damage to the storage tank, and thus various processes are performed on the BOG generated in the storage tank 210. Typically, the BOG may be reliquefied by a reliquefaction device 260 to recover the BOG to the storage tank 210. In another example, the BOG may be re-liquefied by mixing the BOG with the feed gas 10 delivered at high pressure through the suction drum 240. In another example, the BOG may be consumed in the self-generator 280 by using the BOG as a fuel for power generation. In the case where the amount of the excess BOG is large, the BOG is consumed by burning the BOG in the combustion device 290.

Since BOG is consumed by burning an excessive amount of BOG, there is a problem in that chemical energy contained in BOG is consumed by burning. Due to the large amount of CO produced during combustion₂Therefore, there is also a problem of environmental pollution.

FIG. 3 is a block diagram of a reforming system coupled to a feed gas vaporization system according to an embodiment of the present disclosure.

Referring to FIG. 3, a reforming system coupled to a feed gas vaporization system is depicted in accordance with an embodiment of the present disclosure. The reforming system of fig. 3 includes: a raw material gas vaporization system 200 including a storage tank 210 for storing a raw material gas 10 and a transport pipe for transporting the raw material gas 10; the reforming system 100 includes a reformer 120 for generating hydrogen 30 by reacting a raw material gas 10 with water 20, a burner 140 for supplying heat to the reformer 120, and a mixture generated from the reformer 120A PSA130 for separating hydrogen 30 from the gas; CO2₂A separation device 300 for receiving the waste gas from which hydrogen in the mixed gas has been removed from the PSA130 and for causing CO to exchange heat with the transfer line of the raw material gas vaporization system 200₂Liquefaction to remove CO₂(ii) a And a gas supply line 331 for supplying CO₂CO is removed in the separation unit 300₂Is supplied as fuel to the burner 140.

The raw material gas vaporization system according to an embodiment of the present disclosure may cause CO in the exhaust gas generated in the reforming system to be contained in the exhaust gas by a heat exchanger connected to the raw material gas vaporization system₂Liquefaction for CO removal₂. The feed gas vaporization system may include CO₂Separation apparatus 300, CO₂The separation device 300 exchanges heat with the raw material gas vaporization system to make CO included in the exhaust gas before supplying the exhaust gas discharged from the PSA130 to the burner 140 for combustion₂And (4) liquefying.

Since the raw material gas 10 in the raw material gas vaporization system is in a very low temperature liquid state before vaporization, CO₂May be liquefied. To this end, CO₂The separation device 300 may be configured to connect the off-gas discharged from the PSA130 to the raw gas vaporization system 200.

In addition, the reforming system connected to the raw material gas vaporization system according to an embodiment of the present disclosure may further include a BOG supply line 11 through which BOG generated by vaporizing the raw material gas 10 stored in the storage tank 210 is moved. The reformer 120 of the reforming system may be configured to generate hydrogen 30 by using BOG received from the BOG supply line 11 as the raw gas 10 and reacting it with water 20.

As described above, since BOG is generated by vaporizing the raw material gas 10 and is a gas composed of 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 into the reforming system through the BOG supply line 11. The hydrogen 30 may be generated by reforming incoming BOG to generate the hydrogen 30 from the BOG, thereby improving fuel efficiency.

The feed gas vaporization system may further include a BOG compressor 230, the BOG compressor 230 compressing the BOG to flow pressurized (e.g., high pressure) BOG into the BOG supply line 11. BOG compressor 230 may compress BOG to above 1barg and below 10 barg.

Further, the raw material gas vaporization system may include: a first pump 221 connected to the storage tank 210 to compress and deliver the raw material gas 10; and a suction drum 240, a part of the BOG from the BOG passing through the BOG compressor 230 flows into the BOG supply line 11, and the remaining BOG is mixed with the raw material gas 10 fed by the first pump 221, so that the part of the BOG is re-liquefied. The BOG may be re-liquefied by mixing the BOG with the raw gas 10 in the suction drum 240, thereby improving fuel efficiency. The first pump 221 can compress the raw material gas 10 to 1barg or more and 10barg or less.

In addition, the raw material gas vaporization system 200 may further include a second pump 222, and the second pump 222 is connected to the suction drum 240 to compress and transfer the raw material gas 10 passing through the suction drum 240, so that the raw material gas 10 may be compressed to a high pressure. Second pump 222 may compress the feed gas to above 10barg and below 100 barg.

In addition, the raw material gas vaporization system 200 may further include a vaporization device 250, and the vaporization device 250 vaporizes the raw material gas 10 that exchanges heat with the off-gas. The vaporization unit 250 may be various vaporization units 250 for vaporizing LNG. The vaporizing device 250 may include a conventional open rack vaporizer (open rack vaporizer), a submerged burner (submerged combustor), and the like.

The reforming system may include: a water supply device 150 supplying water 20; and a plurality of water heat exchangers 161 to 164 vaporizing water by applying heat thereto and supplying the vaporized water to the reformer 120. The water 20 required for the reforming reaction may be pure water or ultrapure water.

In addition, the reforming system 100 may be configured to further include a mixed gas heat exchanger 170, and the mixed gas heat exchanger 170 is cooled by heat-exchanging the mixed gas passing through the reformer 120 with the coolant. The mixed gas heat exchanger 170 may reduce the temperature of the mixed gas heated during the reforming process. The mixed gas heat exchanger 170 is sized according to the amount of the mixed gas discharged from the reformer 120. For example, as the amount of mixed gas decreases, the size of the mixed gas heat exchanger 170 may also decrease.

In addition, the reforming system 100 may be configured to further include an inverter 180, and the inverter 180 generates the hydrogen 30 by reacting the CO generated in the reformer 120. The shift converter 180 is a device that generates hydrogen 30 by reacting CO with water 20 by the reaction formula described above, and can remove CO and generate hydrogen 30.

FIG. 4 is CO of the reforming system 100 coupled to a raw gas vaporization system according to an embodiment of the disclosure₂Block diagram of the separation apparatus 300. FIG. 5 is a diagram showing CO based reforming system coupled to a raw gas vaporization system according to an embodiment of the present disclosure₂Separation of ambient CO of plant₂Graph of the liquefaction rate of (a). FIG. 6 is a diagram showing CO based reforming system coupled to a raw gas vaporization system according to an embodiment of the present disclosure₂A plot of the efficiency of the reformer system for the ambient conditions of the separation device.

The CO will be described in detail with reference to FIGS. 4 to 6₂A separation device 300.

CO₂The separation device 300 may comprise an exhaust gas compressor 310, a raw gas and exhaust gas heat exchanger 320, CO₂Separator 330 and CO₂A tank 340.

Due to when CO is present₂CO when cooled at a pressure below the triple point₂Sublimes without passing through a liquid state, and thus can be liquefied at a pressure above the triple point and at a temperature above the triple point. CO2₂Has a triple point pressure of 4.2barg and CO₂The triple point temperature of (A) was-57 ℃. Thus, CO₂CO in the separation unit 300₂May be above 4.2barg and CO₂The temperature of (a) may be-57 ℃ or higher.

The offgas compressor 310 is a device that compresses offgas discharged from the PSA130 to a high pressure. The offgas compressor 310 may be connected to the PSA130 to receive offgas.

FIGS. 5 and 6 show CO based on the pressure of the compressed exhaust gas in the exhaust gas compressor 310₂The liquefaction rate and the efficiency of the reformer system. Each graph shows the compression toCO at 50barg (data series 400), compressed to 40barg (data series 500), compressed to 30barg (data series 600), compressed to 20barg (data series 700), and compressed to 10barg (data series 800)₂The liquefaction rate and the efficiency of the reformer system.

Referring to fig. 5, it can be confirmed that CO increases as the pressure of the exhaust gas compressed in the exhaust gas compressor 310 increases₂The liquefaction rate of (3) is increased. Due to the reaction with CO₂The pressure difference between the three phase points of (a) gradually increases with an increase in pressure, and the liquefiable temperature area increases, so that the liquefying rate increases.

Referring to fig. 6, it can be confirmed that the efficiency of the reforming system is reduced when the pressure of the exhaust gas exceeds a certain pressure. As shown in figure 6, the efficiency of the reformer system when compressed to 50barg (data series 400) is lower than when compressed to 30barg (data series 600) and when compressed to 20barg (data series 700) at-40 ℃. This is due to the Joule-Thomson effect, i.e., the CO is reduced by isentropically expanding the compressed, high pressure flue gas as it passes through the narrow bore when injected into combustor 140 through gas supply line 331₂The temperature of (2). Therefore, CO can be considered₂The liquefaction rate and the efficiency of the reformer 120 system to compress the off-gas to an appropriate pressure. For example, the pressure is preferably 20barg or more and 30barg or less.

The raw gas and exhaust gas heat exchanger 320 is a device for exchanging heat between the extremely low temperature raw gas 10 and the exhaust gas. The raw gas and off gas heat exchanger 320 may be connected to a transfer line of the raw gas vaporization system and an off gas supply line. Thus, the raw material gas 10 and CO of the raw material gas vaporization system₂Heat exchange is performed between the exhaust gases of the separation device 300. The CO can be caused by cooling the exhaust gas using the cold heat of the raw material gas 10 as a refrigerant₂And (4) liquefying.

Referring to FIGS. 5 and 6, the lower the cooling temperature of the off-gas when the off-gas exchanges heat with the raw material gas vaporization system, the lower the CO₂The higher the liquefaction rate and the efficiency of the reformer system. However, referring to fig. 6, when the cooling temperature of the exhaust gas is equal to or lower than a certain threshold temperature, the efficiency of the reformer 120 system may be reduced. Therefore, CO should be considered₂The liquefaction rate and the efficiency of the reformer 120 system to cool the exhaust gas to an appropriate temperature. For example, the exhaust gas cooling temperature may be a temperature of-40 ℃ or lower and-50 ℃ or higher.

Therefore, consider CO when referring to fig. 5 and 6₂The liquefaction rate and the efficiency of the reformer system, in one example, CO₂Preferred operating conditions for the separation apparatus 300 are a pressure of 20barg or more and 30barg or less and a cooling temperature of-40 ℃ or less and-50 ℃ or more.

CO₂The separator 330 exchanges heat between the waste gas and the raw gas vaporization system to make CO₂Separation of liquefied CO after liquefaction₂The apparatus of (1). CO2₂The tank 340 is for storing CO liquefied in the exhaust gas₂The apparatus of (1). Can pass through CO₂Separator 330 and CO₂Tank 340 is advantageously used to separately manage the separated and liquefied CO in the flue gas₂。

The raw material gas vaporization system according to the embodiment of the present disclosure may remove CO in the exhaust gas₂Thereby reducing CO of the reformer 120₂And (4) discharging the amount. For example, CO of the reformer 120₂The emission can be reduced by 45%. In addition, due to the removal of CO₂The amount of exhaust gas of the combustor 140 is reduced, and thus the size of the mixed gas heat exchanger 170 can be reduced. For example, the size of the mixed gas heat exchanger 170 may be reduced by 9%. In addition, excess BOG may be used to produce hydrogen 30 rather than being consumed by combustion, thereby improving fuel efficiency.

While the present disclosure has shown and described specific embodiments, it should be apparent to those skilled in the art that various improvements and modifications can be made to the present disclosure without departing from the technical idea of the present disclosure provided by the appended claims.