KR20210085980A - Multi-fuels Reforming system for hydrogen production - Google Patents

Abstract

The present invention relates to a multi-fuel reformer for hydrogen production including an integrated heat exchange system. More specifically, the present invention relates to a multi-fuel reforming system for on-site hydrogen production which can effectively use waste heat from a steam reformer by including a heat source part that generates heat energy, a steam reforming reactor for converting two kinds of raw material gas supplied from the outside into syngas rich in hydrogen gas, a raw material gas supply pipe installed on one side of the steam reformer and for supplying two types of raw material gas, a pre-reforming reactor that is a first preheating zone and a first reaction zone of the steam reforming reactor, and a heat exchanger in a second preheat zone at the bottom.

Description

Multi-fuels Reforming system for hydrogen production

The present invention relates to a reformer of a hydrogen production system, and more particularly, in the case of reforming fuel gas flowing in to obtain hydrogen from fuel gas, preheating and preheating of fuel gas using waste heat used in a heat source of a steam reformer It is a reformer for blue hydrogen production that minimizes waste heat by performing -reforming. It relates to a reformer for hydrogen production that can simultaneously perform preheating, pre-reforming, and reforming of feed gas through a single reformer.

Recently, due to a growing sense of crisis for the global environment, systems using hydrogen as fuel, such as hydrogen fuel cell vehicles, are in the spotlight because of their high energy efficiency and low emission gas in response to the demand for development of an eco-friendly energy supply system.

Among them, as a method of supplying hydrogen in a hydrogen fuel cell vehicle, in addition to a method of directly supplying hydrogen in the form of compression or liquefaction, generation of hydrogen by steam reforming of hydrocarbon fuels such as natural gas is conventional. It is widely used because it can use fuel supply infrastructure such as gas stations and has high overall energy efficiency.

Korean Patent No. 10-0209989 discloses a conventional hydrogen production system for producing hydrogen by reforming hydrocarbon-based fuel gas such as natural gas or liquefied petroleum gas.

Korean Patent Laid-Open No. 10-2014-0120070 relates to a reformer of a hydrogen reforming system, which includes a housing, a heat source provided in the housing and generating heat energy, and a fuel gas provided in the housing and supplied from the outside to hydrogen. A reforming pipe for reforming into gas-rich synthesis gas, a fuel gas supply pipe installed on one side of the housing and supplying fuel gas, an opening/closing means for opening and closing an opened end of the reforming pipe, and the reforming pipe It is connected, characterized in that it comprises a syngas discharge pipe for discharging the reformed syngas.

In Korean Patent Registration No. 10-1943856, a reformer according to an aspect includes an upper housing including a first hole formed in a lower plate; a lower housing including a second hole formed in the upper plate and third to fifth holes formed in the side plate, the lower housing being disposed under the housing; a heater disposed inside the upper housing; a reforming tube including an outer tube and an inner tube disposed inside the outer tube, the reforming tube being disposed in the upper housing and the lower housing, at least a portion of which passes through the first hole and the second hole; a distributor disposed in the lower housing and connected to the outer tube; an inlet gas pipe connected to the distributor and passing through the third hole; an exhaust gas pipe connected to the inner pipe and passing through the fourth hole; and a flue gas discharge pipe passing through the fifth hole.

Such a conventional hydrogen production system includes a desulfurizer for adsorbing sulfur contained in fuel gas, a reformer for reforming the fuel gas that has passed through the desulfurizer to produce a synthesis gas containing abundant hydrogen gas, and a reformer for reforming into a hydrogen-rich gas. It includes a steam generator to obtain the necessary water vapor, and a gas-liquid separator to separate water from the exhaust gas. The reformer is a device for generating hydrogen from a raw material such as natural gas (hereinafter referred to as "raw material gas") through a reforming reaction.

Republic of Korea Patent Publication No. 10-0209989 "Natural gas type hydrogen generator." Korean Patent Laid-Open Publication No. 10-2014-0120070 "Reformer of hydrogen reforming system"

The first object of the present invention is to utilize combustion heat in a hydrogen reforming process to preheat and pre-reforming a supply gas.

In addition, a large amount of waste heat generated in the existing hydrogen reforming process is provided to subsequent units such as preheating, pre-reforming, and water gas conversion processes that require a heat source to maximize the reforming efficiency by minimizing the supply of energy. The purpose.

Furthermore, an object of the present invention is to provide a reforming system for hydrogen production capable of simultaneously performing preheating, pre-reforming, and reforming of raw material gas using a single reformer.

The present invention relates to a reforming system for hydrogen production, and as a preferred embodiment of the present invention, a housing configured to inject raw material gas and to introduce heated air; a heating unit configured to introduce heated combustion gas into the housing; a first preheating region configured so that the supply gas introduced through the first inlet faces the heating unit; a second preheating region configured to face the supply gas introduced through the second inlet and positioned at an upper end of the first preheating region; a first reaction zone in which the feed gas passing through the first preheating zone is converted into methane in a pre-reformer; a second reaction zone in which the feed gas preheated through the second preheating zone and the downstream gas of the pre-reformer of the first reaction zone are mixed to produce synthesis gas by methane steam reforming; The first reaction zone and the first reaction zone are configured to face the heating part by mixing the syngas discharged through the first reaction zone and the first reaction zone, and configured to discharge the syngas generated through the second reaction zone and a hydrogen reforming system including a heating unit and a heating chamber for supplying a heat source to the second reaction zone.

In addition, the first inlet and the second inlet are configured in an annular shape, and include a reforming system for hydrogen production configured to be connected by supplying a reaction gas to the first reaction zone and the second reaction zone, respectively.

The first reaction zone or the second reaction zone also includes a reforming system for hydrogen production configured to include at least one or more nipples.

In addition, the heating unit may include: a heating conduit configured to pass through the first reaction region and the second reaction region; and a multi-fuel reforming system configured to include a heating chamber configured to provide heat to the first and second reaction zones.

In addition, the first reaction zone and the second reaction zone include a multi-fuel reforming system for hydrogen production that is separated from each other through a separator or is integrally configured.

In addition, the discharge part of the first reaction zone includes a multi-fuel reforming system for hydrogen production configured to be organically connected to the second reaction zone.

In addition, the lower end of the reaction conduit forming the second reaction region is configured to be in fluid communication with the first reaction region, and the stop of the reaction conduit is configured to be in fluid communication with the second preheating region. reforming system.

In addition, the first reaction zone and the second reaction zone include a multi-fuel reforming system for hydrogen production configured to perform preheating in response to the reaction temperature of the raw material gas.

In addition, the third reaction region may include: a pre-reforming conduit fluidly connected to the first reaction region; It features a multi-fuel reforming system for hydrogen production configured to include; a reforming conduit configured to be in fluid communication with the discharge end of the second reaction zone and the pre-reforming conduit.

According to the present invention, the combustion heat for multi-fuel reforming is used as a heat source for preheating, pre-reforming and reforming of the reaction raw material gas supply pipe, and the waste heat of the combustion gas is used in the process of supplying a heat source necessary for other purification of high-purity hydrogen gas. As a result, it is possible to minimize the waste heat of a large amount of combustion gas generated in the multi-fuel reforming process, thereby maximizing the reforming efficiency of the reformer.

In addition, since the integrated multi-fuel reforming process can be performed through one reformer, it is possible to simplify the facility (compact) and provide maintenance convenience.

In addition, since the present invention enables the design of a compact reformer through the on-site multi-fuel reforming system for hydrogen production that provides one reformer, it has an effect of high spatial utilization when constructing a hydrogen station on the on-site.

1 is a cross-sectional side view of a hydrogen reforming system for minimizing waste heat as an embodiment of the present invention.

A preferred embodiment of the present invention will be described in detail with reference to the accompanying drawings. Advantages and features of the present invention, and methods for achieving them, will become apparent with reference to the accompanying process drawings. However, the present invention is not limited to the embodiments disclosed below and may be implemented in various different forms. Like reference numerals refer to like elements throughout.

Unless otherwise defined, all terms (including technical and scientific terms) used herein may be used with the meaning commonly understood by those of ordinary skill in the art to which the present invention belongs. In addition, the terms defined in the dictionary used in general are described below in a direction that is not ideally or excessively interpreted unless clearly defined in particular. In addition, the terminology used in this specification is for the purpose of helping understanding, and is not intended to limit the present invention. As used herein, the singular also includes the plural unless specifically stated otherwise in the phrase. As used herein, to include and/or to include is used in a sense that does not exclude the presence or addition of one or more other components, steps and/or actions in addition to the stated components, steps and/or actions. And, “and/or” includes each and every combination of one or more of the recited elements.

The steam reforming conduit (second reaction region) 400, the heating conduit is made of, the synthesis gas from the reforming conduit 400 is a water gas conversion unit for water gas shift reaction (WGS) of carbon monoxide, gas -Provides an apparatus for producing high-purity hydrogen by steam reforming, including a liquid separation unit and a PSA unit (Pressure Swing Adsorption) for hydrogen separation.

More preferably, the syngas reformed through the steam reforming reaction is configured to be connected to the WGS unit, the gas-liquid separation unit and the PSA unit through the syngas discharge unit 450 of the multi-fuel reforming system.

As the hydrocarbon feedstock, LNG is used in this example, but is not limited thereto, and the raw material may be gaseous hydrocarbons such as LNG, LPG, and Biogas, or liquid hydrocarbons including Naphtha, gasoline, and diesel. The gaseous fuel is divided into two parts: a feed and a fuel, the reaction raw material is provided to the reformer after passing through the desulfurization unit, and the fuel is provided to the heating unit 200 . The liquid hydrocarbon may be supplied in the gas phase after vaporization by utilizing the waste heat of the combustion gas.

In the present invention, as a desulfurization method of raw hydrocarbons, a method of removing sulfur compounds by hydrodesulfurization and then removing them in an adsorption tower or directly adsorbing them in an adsorption tower can be used. In this case, as the adsorbent, for example, a metal such as cobalt, zinc, copper, or an oxide thereof, or an emulsion, and further, a zeolite or activated carbon may be used.

의 온도에서 고온 수첨탈황을 통해 제거할 수도 있다.It can be adsorbed and removed at room temperature using zeolite or activated carbon, and 300 to 400 depending on the feedstock and conditions.

It can also be removed through high-temperature hydrodesulphurization at a temperature of

의 온도까지 예열되도록 구성된다. This selectively desulfurized feedstock is fed to the first or second inlet of the present invention and then 450 to 500 through the heat exchangers in the first preheating zone and the second preheating zone to conform to the reforming reaction.

It is configured to be preheated to a temperature of

In an embodiment of the present invention, the temperature of the reaction raw material gas is increased through the first preheating region 800 and the second preheating region 700 to conform to the reformer reaction, and the bar heated by the heating unit 200 is heated. The exhaust gas discharge unit 550 is configured such that the exhaust gas passes through the first preheating region 800 and the second preheating region 700 and is discharged to the outside.

More preferably, the heating unit 200 includes a heating conduit configured to pass through the first preheating region 800 and the second preheating region 700 and a heating chamber 900 configured to face at least a portion of the first reaction region. is composed of Further, the heating chamber 900 may be configured to face the reforming conduit 400 of the second reaction region.

The heating chamber 900 is configured such that the heat source of the heating unit 200 is transmitted directly or indirectly. In an embodiment of the present invention, the side partition wall and the heating conduit are configured to surround the discharge unit 410 located on both sides of the housing. It may be configured to include a vertical partition wall positioned between the 500 and the heating unit 200 .

The heat source of the heating unit 200 is bypassed through the side partition wall and the vertical partition wall to provide heat at an appropriate temperature to the second reaction zone 400 , the first preheat zone 800 , and the second preheat zone 700 . .

2 The fuel to be reacted flowing into the reaction zone (reforming reactor) may be composed of a single conduit or a double conduit, and the form is not limited.

The fuel to be reacted flowing into the second reaction zone (reforming reactor) may be configured as a single conduit or a double conduit, and the form is not limited thereto.

In addition, the second reaction zone (reforming reactor) is configured to move the feedstock introduced upwards of the housing, and is configured to be inverted to move downwardly and discharged.

As described above, by performing the temperature increase by heat exchange, the raw material moisture contained in the reaction raw material mixture does not flow into the hydrogen reforming system 100 in a state separated into two phases, a liquid and a gaseous phase, and is vaporized after sufficient vaporization. can be introduced into the reforming reaction while maintaining a single phase of It is possible through the proper design of the heat exchanger considering the vaporization temperature of moisture.

That is, when a conduit capable of supplying the pressure applied to moisture and the amount of heat capable of raising the temperature to a temperature higher than the vaporization point at the pressure from the exhaust gas after combustion is provided inside the housing, and an appropriate amount of exhaust gas is supplied A single phase of continuous water vapor can be maintained.

The raw material introduced into the reformer may be subjected to a desulfurization process before being supplied to the reformer (housing).

The reforming unit (reforming conduit 400) contacts the mixture of the reaction raw materials with a reforming catalyst and performs steam reforming, thereby producing a high-concentration hydrogen-containing gas. A heating unit 200 configured to transfer heat to the inside of the reforming unit is provided at an upper portion of the reforming unit.

Examples of the reforming catalyst include those in which a metal such as nickel or ruthenium is supported on a carrier such as alumina, silica, or magnesium aluminate. Steam reforming of desulfurized hydrocarbons in the reforming unit is performed by the following reaction formula.

CO + 3H ₂ ↔ CH ₄ + H ₂ O --- (Steam Reforming, SR)

CO + H ₂ O ↔ CO ₂ + H ₂ --- (Water Gas Shift, WGS)

It is configured to supply the heat source inside the reformer through the heating unit 200 located at the top of the housing, and more preferably, to the heating unit 200 via the second preheating region 700 and the first preheating region 800 . The exhaust gas of the fuel burned by the exhaust gas is configured to be discharged to the outside of the housing through the exhaust gas discharge unit (550).

After the exhaust gas is discharged as much as waste heat is recovered by the heat exchanger, _{it may be configured to be fluidly connected to the CO 2} recovery device, and may be configured to recirculate the unburned hydrocarbon gas to the heating unit 200 .

The lower surface of the housing includes a source gas inlet 600 configured in the form of an annular conduit, and the fuel gas introduced into the source gas inlet 600 is a first preheating region 800 and a second preheating region 700 . is configured to flow into

More preferably, the supply amount of the valve located at one end of the inlet can be controlled according to conditions such as the temperature of the raw material gas, so that the amount of the raw material gas flowing into the first preheating region 800 and the second preheating region 700 is controlled. The flow rate can be controlled.

Furthermore, different fuel gases may be provided to the first preheating region 800 and the second preheating region 700 .

In an embodiment of the present invention, the first preheating region 800 and the second preheating region 700 may be divided into regions in which preheating is performed to increase the temperature of the raw material gas before the reaction.

In addition, it may be divided into a first reaction region 300 that faces the discharge end of the first preheating region 800 and performs pre-reforming of the source gas.

That is, the first reaction region 800 is configured such that the raw material gas introduced to the outside of the annular conduit of the fuel gas inlet 600 is introduced, and through the exhaust gas conduit of the heater through a plurality of nipples, the first reaction region is configured to flow into the Pre-Reforming reactor 300 . However, the pre-reforming reactor includes a hydrogen reforming system in which a catalyst may be charged if necessary depending on the type of the raw hydrocarbon gas, otherwise the preheated gas movement path is included.

More preferably, the outside of the annular conduit outside the fuel gas inlet 600 is the first raw material gas inlet 610, and fuels such as LPG, gasoline, diesel and glycerol that require pre-reforming are introduced into the first reaction region. It is configured to be introduced into the Pre-Reforming reactor (300).

The second preheating region 700 is located at the upper end of the first preheating region 800 so that the raw material gas introduced through the central part of the annular conduit of the raw material gas inlet 600 is introduced, and the raw material gas introduced through at least one nipple. It is configured to set the path.

The raw material gas passing through the second raw material region 700 is configured to flow to one end of the pre-reforming reactor 300 and the reforming reactor 400 facing each other to perform a steam reforming reaction along the reforming conduit 400 .

More preferably, the central portion of the conduit outside the fuel gas inlet 600 is configured to introduce methane-based gases (NG, CNG, LNG and reactor off gas) as the second source gas inlet 620, the reforming reactor 400 is configured to flow into

In addition, the reaction raw material that does not require pre-reforming is supplied to the first preheating area 800 and the second preheating area 700 through the first fuel gas inlet 610 and the second fuel gas inlet 620 . The reaction fuel that can be introduced and that requires pre-reforming is configured to be introduced through the first fuel gas inlet 610 to be introduced into the first preheating region 800 .

The pre-reforming reactor 300 and the reforming reactor 400 are configured to be located in the first reaction zone and the second reaction zone, and each of the pre-reforming reactor 300 and the reforming reactor 400 is filled with a catalyst. The reforming reaction is configured to occur.

More preferably, as the steam reforming catalyst, a metal such as nickel or ruthenium is supported on a carrier such as alumina, silica, and magnesium aluminate, and the like.

The second reaction zone 400 is configured to be adjacent to a heat source having a higher temperature than the first reaction zone 300 , the first preheat zone 800 , and the second preheat zone 700 , and more preferably, the second reaction zone 400 . The reforming conduit 400 in the region may be formed in the longitudinal direction along the top of the housing so that the temperature applied from the heat source has a maximum value at the uppermost end of the reforming conduit 400 .

More preferably, it is configured to be separated into two regions by a partition wall positioned in the heating chamber, and a heat source can be indirectly introduced into the region where the reforming conduit 400 is positioned.

Accordingly, the syngas reacted through the reforming conduit 400 may be discharged through the discharge unit 410 including at least one on both sides of the housing.

The synthesis gas thus discharged can store high-purity hydrogen through at least one of a water gas conversion unit for a water gas shift reaction (WGS) of carbon monoxide, a gas-liquid separation unit, and a PSA unit for hydrogen separation. is configured to

를 갖도록 구성될 수 있다.In an embodiment of the present invention, the temperature of the heat source transferred to the reforming reactor 400 is 750 to 900

It can be configured to have

In summary, the fuel gas passing through the first preheating region 800 and the second preheating region 700 includes the first reaction region 300 and the second reaction region 400 for performing pre-reforming or reforming. As configured, the second reaction zone is composed of a main reaction zone in which steam reforming of the raw material gas is performed.

The second reaction area is located above the first preheating area 800 and the second preheating area 700 , and positioned at the rear end of the first preheating area 800 , the first reaction area 300 and the second reaction area for pre-reforming. It is configured to receive the preheated raw material gas discharged from the preheating region 700 to perform a steam reforming reaction.

Although the configuration of the present invention has been described with reference to the accompanying drawings, those of ordinary skill in the art to which the present invention pertains will realize that the present invention may be implemented in other specific forms without changing the technical spirit or essential features thereof. You will understand. Therefore, it should be understood that the contents described above are exemplary in all respects and not specifically stated.

100: multi-fuel reforming system for hydrogen production
200: heating unit
300: first reaction zone: Pre-Reforming reactor
400: second reaction zone: reforming reactor
450: syngas discharge unit
500: heating conduit
550: exhaust gas discharge unit
600: reaction raw material gas inlet
610: first source gas inlet
620: second source gas inlet
700: second preheating region
800: first preheating region
900: heating chamber

Claims (10)

a housing for multi-material reforming configured to inject raw material gas for on-site hydrogen production and to introduce fuel gas and air;
a heating unit configured to introduce heated source gas into the housing;
a first preheating region configured so that the raw material gas introduced through the first raw material inlet faces the heating unit;
a second preheating region configured to face the source gas introduced through the second raw material inlet to face the heating unit and positioned above the first preheating region;
The reaction gas of the first reaction region in which the pre-reforming reaction is performed through the first preheating region and the raw material gas discharged through the second preheating region are mixed and configured to face the heating unit, and heated in the second reaction region A multi-fuel reforming system for hydrogen production in which the exhaust unit for discharging synthesis gas synthesized by steam reforming reaction through the unit and the reformed synthesis gas are linked with the WGS unit, the gas-liquid separation unit and the PSA unit. The method of claim 1,
The first raw material inlet and the second raw material inlet have an annular shape, and are configured to be in fluid communication with the first preheating region and the second preheating region, respectively. The method of claim 1,
A multi-fuel reforming system for hydrogen production configured to include at least one nipple in the first preheat zone or the second preheat zone. The method of claim 1,
The heating unit,
a heating conduit configured to pass through the first preheat region and the second preheat region;
and a heating chamber configured to provide heat to the first reaction zone and the second reaction zone. The method of claim 1,
The multi-fuel reforming system for hydrogen production is configured such that the first preheating region and the second preheating region are divided from each other through a separator. The method of claim 1,
and the discharge portion of the first preheating zone is configured to be supplied to the first reaction zone and then in fluid communication with the second reaction zone. The end of the steam reformer forming the second reaction region is configured such that the source gas preheated in the first preheating region is fluidly connected to the first reaction region,
The inlet of the steam reforming reactor is configured to be in fluid communication with the second preheat zone and the first reaction zone to be mixed. According to claim 1,
The first preheating region and the second preheating region are configured to perform preheating in response to a reforming reaction temperature of the source gas. According to claim 1,
The second reaction region is
a pre-reforming reactor in fluid communication with the first preheating zone;
and a steam reforming reactor configured to be in fluid communication with the second preheating zone and an outlet end of the pre-reforming reactor. According to claim 1,
Syngas discharged from the housing of the steam reformer is a multi-fuel reforming system for high-purity hydrogen production through the WGS unit, the gas-liquid separation unit and the PSA unit.

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