KR101747516B1 - Heat exchanging device of hydrogen producing apparatus - Google Patents

Heat exchanging device of hydrogen producing apparatus Download PDF

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Publication number
KR101747516B1
KR101747516B1 KR1020150059455A KR20150059455A KR101747516B1 KR 101747516 B1 KR101747516 B1 KR 101747516B1 KR 1020150059455 A KR1020150059455 A KR 1020150059455A KR 20150059455 A KR20150059455 A KR 20150059455A KR 101747516 B1 KR101747516 B1 KR 101747516B1
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South Korea
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heat exchanger
pipe
combustion gas
supplied
outlet
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KR1020150059455A
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Korean (ko)
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KR20160128487A (en
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이영철
한정옥
이중성
김용철
조영아
김형태
김상민
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한국가스공사
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/508—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by selective and reversible uptake by an appropriate medium, i.e. the uptake being based on physical or chemical sorption phenomena or on reversible chemical reactions
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C01B3/58—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids including a catalytic reaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/007—Auxiliary supports for elements
    • F28F9/013—Auxiliary supports for elements for tubes or tube-assemblies

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

The present invention relates to a heat exchanger of a hydrogen production apparatus, and includes a boiler (120) and first to fourth heat exchangers (130, 140, 150 and 160) in a case (110). The boiler 120 and the first to fourth heat exchangers 130, 140, 150, and 160 heat-exchange natural gas and water supplied from the outside with synthesis gas and combustion gas generated from the reformer, raise the temperature to an appropriate temperature, and supply the reformed gas to the reformer. The heat exchanger is integrated in the case and the length of the pipe pipe is reduced, so that the heat loss is reduced and the energy efficiency is improved.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a heat exchanging device of a hydrogen producing apparatus,

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a heat exchange apparatus for a hydrogen production apparatus, and more particularly, to a heat exchange apparatus for use in an apparatus for producing hydrogen gas from natural gas.

Generally, a hydrogen producing apparatus for producing hydrogen using natural gas includes a reformer, a conversion reactor, a pressure swing adsorption (PSA) apparatus, and a heat exchange apparatus.

In the reformer, the desulfurized natural gas and water vapor undergo a reforming reaction by the burner heating and catalytic action to produce the primary syngas.

In the conversion reactor, the carbon monoxide is removed through the aqueous transition reaction to produce a second synthesis gas having a higher hydrogen content.

Synthetic gas 2 is supplied to the PSA unit and removes impurities including carbon monoxide by pressure swing adsorption process to produce high purity hydrogen gas.

The heat exchanging device exchanges the natural gas, water or steam (DI-Water), the primary syngas, and the secondary syngas with each other when the devices move, thereby satisfying the temperature condition of the fluid entering each device, Thereby improving the energy efficiency of the device.

As described above, Japanese Patent Application No. 2008-504151 discloses a prior art for heating water and methane-containing gas through heat exchange with combustion waste in a hydrogen producing apparatus for producing hydrogen gas from a methane-containing gas.

On the other hand, the conventional heat exchanger of the hydrogen producing apparatus has a poor heat exchange efficiency and often fails to satisfy the inlet temperature condition of each fluid. Particularly, since the temperature of the natural gas and steam supplied to the reformer is not sufficiently increased, the reaction performance of the reformer is deteriorated, and the amount of fuel used in the burner is increased in order to recover it.

In addition, since the heat exchangers constituting the heat exchanger are dispersedly arranged, the installation area of the hydrogen generator is increased and the amount of connected piping is increased, thereby increasing the amount of heat loss and inconveniencing inspection and repair.

Accordingly, the present invention has been devised to solve the above-mentioned problems, and it is an object of the present invention to provide a heat exchanger in which a plurality of heat exchangers are installed adjacent to each other in a case to reduce heat loss in a connection pipe, improve heat exchange efficiency between fluids, The present invention has been made in view of the above problems, and it is an object of the present invention to provide a heat exchanging device for a hydrogen producing apparatus which is easy to inspect and repair.

According to an aspect of the present invention, there is provided a reforming apparatus for reforming natural gas, comprising: a reformer for generating a primary synthesis gas containing hydrogen through steam reforming of natural gas; A PSA apparatus for generating high-purity hydrogen gas by further removing impurities from carbon monoxide by pressure swing adsorption, and a reforming unit for reforming natural gas A water supply unit for supplying water vapor to the reformer; and a heat exchanger for exchanging the natural gas and the water with the combustion gas discharged from the reformer and the reforming reactor, the primary syngas and the secondary syngas to satisfy the inlet temperature condition of the reformer And a heat exchanger for heating the heat exchanger.

The heat exchanger includes a case, a boiler installed at one side of the case, and a first heat exchanger, a second heat exchanger, a third heat exchanger, and a fourth heat exchanger installed at a side of the boiler inside the case.

The case is provided with a heat insulating material on its inner surface.

The case may be partially open at its side.

The boiler is provided with a first synthesis gas inlet, a first synthesis gas outlet, a combustion gas inlet, and a combustion gas outlet, and a tank portion filled with water, And the primary syngas discharge line is connected to the primary syngas line, the combustion gas discharge line and the combustion gas discharge line are connected to the combustion gas line, the primary syngas line and the combustion gas line are installed in the inside of the tank part in an inverted U- The water in the tank is heated by the primary synthesis gas flowing through the primary syngas and the combustion gas flowing through the combustion gas pipe to generate steam, and the steam is supplied to the reformer through a pipe connected to the upper portion of the tank.

The primary syngas discharged from the primary syngas discharge portion of the boiler is supplied to the conversion reactor through the pipe and the secondary syngas discharged from the conversion reactor is supplied to the inlet of the shell side portion of the secondary heat exchanger through the pipe The secondary syngas discharged from the outlet of the shell side of the secondary heat exchanger is supplied to the inlet of the shell side of the tertiary heat exchanger through the pipe and the secondary synthesis gas discharged from the outlet of the shell side of the tertiary heat exchanger Gas is supplied to the inlet of the PSA device through the pipe.

One end of the tubes constituting the tube side portion of the first heat exchanger is directly connected to the combustion gas discharge portion of the boiler so that the combustion gas discharged from the combustion gas discharge portion flows directly into the tube side portion of the first heat exchanger, The combustion gas discharged from the tube side outlet of the fourth heat exchanger is supplied to the tube side inlet of the fourth heat exchanger through the pipe and the combustion gas discharged from the tube side outlet of the fourth heat exchanger is discharged to the atmosphere through the pipe do.

The water discharged from the outlet of the water supply portion is supplied to the inlet of the shell side portion of the first heat exchanger so that the water is firstly heated by the combustion gas.

The water discharged from the shell side portion outlet of the first heat exchanger is supplied to the inlet of the tube side portion of the second heat exchanger through the pipe so that the water is secondarily heated by the second synthesis gas, And the water discharged from the outlet is supplied to the tank portion of the boiler through the pipe.

The natural gas discharged from the outlet of the natural gas supply portion is supplied to the inlet of the shell side portion of the fourth heat exchanger through the pipe so that the natural gas is firstly heated by the combustion gas and discharged at the shell side portion outlet of the fourth heat exchanger The natural gas is supplied to the inlet of the tube side portion of the third heat exchanger through the pipe so that the natural gas is secondarily heated by the second synthesis gas and the natural gas discharged from the tube side portion outlet of the third heat exchanger And is supplied to the reformer through the reformer.

Three of the first to fourth heat exchangers may be stacked one on top of the other and one of the other may be installed on the bottom plate of the case.

Three of the first to fourth heat exchangers form one row and are stacked one on top of the other and the other one is formed in a different row, a support frame is installed on a bottom plate of the case, Can be installed on the upper part of the frame.

Two of the first to fourth heat exchangers may be stacked one on top of the other and the other two may be stacked on top of each other.

The first to fourth heat exchangers are formed in the shape of a rectangular tube so that the lower surface of the upper heat exchanger and the upper surface of the lower heat exchanger directly contact each other in a planar state during lamination.

As described above, according to the present invention, the heat exchange efficiency of the heat exchanger is improved and the inlet temperature condition of each reactor can be satisfied, so that the reaction efficiency is improved and the yield and purity of the hydrogen gas are improved. Particularly, the temperature of the natural gas and steam supplied to the reformer is sufficiently increased, so that the reforming reaction is smoothly performed and the fuel consumption of the reformer burner is reduced.

Further, since the heat exchangers constituting the heat exchanger are integrally installed in one case, the installation area of the hydrogen generator is reduced, the amount of connected piping is reduced, and the amount of heat loss is reduced.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a configuration diagram of a heat exchanger of a hydrogen producing apparatus according to the present invention; FIG.
2 is a diagram illustrating an example of an installation state of individual heat exchangers constituting the heat exchanger.
Fig. 3 is an example of an installation state when the individual heat exchangers are in the shape of a square tube.

While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawings and will herein be described in detail. It should be understood, however, that the invention is not intended to be limited to the particular embodiments, but includes all modifications, equivalents, and alternatives falling within the spirit and scope of the invention. The thicknesses of the lines and the sizes of the components shown in the accompanying drawings may be exaggerated for clarity and convenience of explanation.

In addition, the terms described below are defined in consideration of the functions of the present invention, and these may vary depending on the intention of the user, the operator, or the precedent. Therefore, definitions of these terms should be made based on the contents throughout this specification.

Hereinafter, preferred embodiments according to the present invention will be described in detail with reference to the accompanying drawings.

First, a configuration of a hydrogen producing apparatus to which a heat exchanging apparatus according to the present invention is applied will be briefly described with reference to FIG.

The hydrogen production apparatus comprises a reformer (not shown) for producing a primary synthesis gas (G1) containing hydrogen through a steam reforming reaction (CH4 + H20 = CO + 3H2 + 49.7 Kcal / mol) A conversion reactor 200 for producing a second synthesis gas G2 having increased hydrogen content through an aqueous transition reaction (CO + H2O = CO2 + H2 - 10 Kcal / mol), a second synthesis gas A pressure swing adsorption (PSA) apparatus 300 for removing carbon monoxide (CO) and impurities by pressure swing adsorption to generate high purity hydrogen gas, a natural gas supply unit 400 for supplying natural gas to the reformer, A water supply unit 500 for supplying water vapor to the reformer, heat exchange between the natural gas and water with the combustion gas discharged from the reformer and the conversion reactor 200, the primary synthesis gas and the secondary synthesis gas, And a heat exchange device 100 according to the present invention for heating to satisfy the conditions.
The reformer, the conversion reactor 200, the PSA apparatus 300, the natural gas supply unit 400, and the water supply unit 500 are installed outside the heat exchange apparatus 100.

The reformer has a burner, and is supplied with natural gas as fuel for the burner. In addition, the reformer is supplied with natural gas and water vapor as a reforming reaction unit carrying a catalyst. The natural gas supplied to the reforming reaction part serves as a raw material for hydrogen gas production.

The conversion reactor 200 also has a reaction catalyst therein and has an electrothermal heater (not shown) for activating the catalyst. The conversion reactor 200 receives the primary syngas G1 discharged from the reformer and lowers the content of carbon monoxide through the aqueous transition reaction to produce a secondary syngas G2 having an increased hydrogen content.

The PSA device 300 includes an adsorbent material therein to adsorb and remove carbon monoxide and other impurities in the secondary syngas G2 under a high pressure condition to produce hydrogen gas of higher purity due to the difference in adsorbability between materials.

The natural gas supply unit 400 includes a desulfurization facility for removing sulfur components from natural gas, a tank for storing the desulfurized natural gas, and valves for controlling the supply flow rate and the supply pressure.

The water supplied from the water supply unit 400 is deionized water from which ions have been removed by passing a constant water through the ion exchange resin to remove ions. The water supply part 400 also includes a storage tank, valves for controlling the supply flow rate and the supply pressure.

The heat exchanging apparatus 100 according to the present invention includes a case 110, a boiler 120 installed inside the case 110, and a plurality of heat exchangers 130, 140, 150, and 160.

The case 110 has a rectangular parallelepiped shape and is provided with a door on each surface so that the upper surface and one or more side surfaces can be opened, or the plate material itself constituting the side surface can be removed.

In addition, a heat insulating material (not shown) may be installed on the inner surface of the case 110 so as to insulate the inside and the outside of the case 110. Therefore, the heat inside the case 110 is not radiated well to the outside.

The boiler 120 is installed in an upright position on one side inside the case 110. A first synthesis gas inlet 121, a first synthesis gas outlet 122, a combustion gas inlet 123 and a combustion gas outlet 124 are formed in a lower portion of the boiler 120, That is, the tank portion is filled with water. The primary syngas inlet 121, the primary syngas outlet 122, the combustion gas inlet 123, and the combustion gas outlet 124 are partitioned.

The primary synthesis gas pipe 125 and the combustion gas pipe 126 are installed in the tank portion. The primary syngas pipe 125 is positioned inside the combustion gas pipe 126 to connect the primary syngas inlet 121 and the primary syngas outlet 122 and the combustion gas pipe 126 is connected to the primary synthesis And is connected to the combustion gas inlet 123 and the combustion gas outlet 124 by being positioned outside the gas pipe 125. The primary syngas pipe 125 and the combustion gas pipe 126 may each be a tube bundle composed of a plurality of pipes.

The water is filled to such an extent that the primary syngas pipe 125 and the combustion gas pipe 126 are submerged, and the empty space above the tank portion filled with water is utilized as a space where water evaporates and water vapor is filled.

Heat exchangers (130, 140, 150, 160) are installed in the other space of the case (110). The heat exchangers 130, 140, 150 and 160 are shell and tube type heat exchangers.

The shell-and-tube heat exchanger is generally cylindrical in shape and includes a pair of tube side portions connected by a plurality of tubes, and a shell side portion formed by baffles in the both tube side portions to form independent spaces. The plurality of tubes are installed in such a structure as to connect the two tube side portions via the shell side portions. The shell side portion and the tube side portion are provided with an inlet and an outlet, respectively.

The plurality of heat exchangers 130, 140, 150 and 160 are a first heat exchanger 130, a second heat exchanger 140, a third heat exchanger 150 and a fourth heat exchanger 160.

1, the first heat exchanger 130, the second heat exchanger 140, the third heat exchanger 150, and the fourth heat exchanger 160 may be stacked as a whole, And can be installed in various layout structures.

The first heat exchanger 130 is installed in a structure directly connected to one lower end of the boiler 120 and mounted on the bottom plate 111 of the case 110 (see FIG. 2). In the case of the first heat exchanger 130, since the tubes are directly connected to the combustion gas discharge portion 124 of the boiler 120, the one side tube side portion is removed. That is, the first heat exchanger 130 shares the combustion gas discharge portion 124 and serves as an inlet portion of the tube side portion.

A second heat exchanger 140 is installed on the upper portion of the first heat exchanger 130 and a third heat exchanger 150 is installed on the upper portion of the second heat exchanger 140, And a fourth heat exchanger 160 may be installed on the upper portion.

A mounting member 170 is provided between each heat exchanger to support and fix the upper heat exchanger to the lower heat exchanger. The mounting member 170 will be described later with reference to Fig.

The primary syngas outlet of the reformer is connected to the primary syngas inlet 121 of the boiler 120 by a pipe P1.

The primary syngas discharge portion 122 of the boiler 200 is connected to the inlet of the conversion reactor 200 by a pipe P2.

The outlet of the conversion reactor 200 is connected to the shell side inlet of the second heat exchanger 140 by a pipe P3.

The outlet of the shell side portion of the second heat exchanger (140) is connected to the inlet of the shell side portion of the third heat exchanger (150) by a pipe (P4).

The outlet of the shell side of the third heat exchanger 150 is connected to the inlet of the PSA apparatus 300 by a pipe P5.

The combustion gas outlet of the reformer is connected to the combustion gas inlet 123 of the boiler 120 by a pipe P6.

The combustion gas discharge portion 124 of the boiler 120 is directly connected to one side of the tube of the first heat exchanger 130.

The tube side portion outlet of the first heat exchanger 130 is connected to the tube side portion inlet of the fourth heat exchanger 160 by a pipe P7.

A pipe P8 is connected to an outlet of the tube side of the fourth heat exchanger 160. The pipe P8 passes through the case 110 of the heat exchanger 100 and communicates with the atmosphere.

The outlet of the water supply unit 500 is connected to the shell side inlet of the first heat exchanger 130 by a pipe P9.

The shell side portion outlet of the first heat exchanger 130 is connected to the tube side portion inlet of the second heat exchanger 140 by a pipe P10.

The outlet of the tube side portion of the second heat exchanger 140 is connected to the inlet of the tank portion of the boiler 120 by a pipe P11.

A pipe P12 extending through the case 110 of the heat exchanger 100 and extending to the outside is connected to the outlet of the tank portion of the boiler 120. [

The outlet of the natural gas supply unit 400 is connected to the shell side inlet of the fourth heat exchanger 160 by a pipe P13.

The outlet of the shell side portion of the fourth heat exchanger 160 is connected to the inlet of the tube side portion of the third heat exchanger 150 by a pipe P14.

The outlet of the tube side portion of the third heat exchanger 150 passes through the case 110 of the heat exchanger 100 and is connected to the natural gas inlet of the reformer through a pipe P15.

The pipe P12 connected to the outlet of the tank of the boiler 120 is connected to the pipe P15 connected to the natural gas inlet of the reformer.

Meanwhile, the first to fourth heat exchangers 130, 140, 150 and 160 may be arranged in various structures as shown in FIG. 2 while maintaining the pipe connection structure as described above.

2 (a) shows a first heat exchanger 130 mounted on one side of a bottom plate 111 of a case 110, and a second heat exchanger 140 mounted on an upper portion of the first heat exchanger 130 The third heat exchanger 150 is mounted on the upper portion of the second heat exchanger 140 while the fourth heat exchanger 160 is installed on the side of the first heat exchanger 130 of the bottom plate 111 to be.

2B is a sectional view of the second heat exchanger 140. The second heat exchanger 140 is mounted on the upper portion of the first heat exchanger 130 and the third heat exchanger 150 is mounted on the upper portion of the second heat exchanger 140, A support frame 180 is installed on the side of the first heat exchanger 130 of the plate 111 and a fourth heat exchanger 160 is installed on the upper side of the support frame 180. The height of the fourth heat exchanger 160 is raised by the support frame 180 and disposed on the side of the second heat exchanger 140.

2 (c) shows a structure in which two heat exchangers are stacked in each column. A second heat exchanger 140 is mounted on the upper portion of the first heat exchanger 130, and a second heat exchanger The fourth heat exchanger 160 is mounted on the side of the third heat exchanger 130 and the third heat exchanger 150 is mounted on the upper portion of the fourth heat exchanger 160. [

In the above-described heat exchanger arrangement structure, the mounting of the heat exchanger is carried out via the mounting member 170. The mounting member 170 includes an upper mounting plate 171 fixed to the lower portion of the upper heat exchanger and a lower mounting plate 171 fixed to the upper portion of the lower heat exchanger (the upper surface of the bottom plate in the case of a heat exchanger installed on the bottom plate) And a bolt 173 penetratingly connected to both ends of the upper mounting plate 171 and the lower mounting plate 172.

The upper mounting plate 171 and the lower mounting plate 172 are fixed to the heat exchanger or the floor by bolting or welding. It goes without saying that a nut is fastened to the lower end of the bolts 173 on both sides.

The upper mounting plate 171 and the lower mounting plate 172 may be connected by bolts 173 in a state where they are directly abutted with each other or between the upper mounting plate 171 and the lower mounting plate 172 by a support block 174, The distance and space between the heat exchanger (or the bottom plate) can be secured. This distance and space can be used to secure the installation space of the pipes constituting the pipeline.

Meanwhile, as shown in FIG. 3, the heat exchangers 130, 140, 150, and 160 may be formed in a rectangular tube shape. In this case, since the mounting plate is not used as the construction of the mounting member 170 ', the upper surface and the lower surface of each heat exchanger are flat, and the stability in the stacking of the heat exchanger is improved. Therefore, a mounting flange projecting horizontally on both sides of the heat exchanger is applied can do. In other words, an upper mounting flange 171 'is formed on both sides of the lower end of the upper heat exchanger, a lower mounting flange 172' is formed on both upper ends of the lower heat exchanger, and the upper mounting flange 171 ' (172 ') is connected via a bolt (173'). At this time, it is of course possible to secure a necessary distance and space between the heat exchanger and the heat exchanger or between the heat exchanger and the bottom plate 111 via a support block (not shown) between the upper heat exchanger and the lower heat exchanger.

3 (a), 3 (b), and 3 (c) show only the shape of the heat exchanger (circular tube and square tube) The description of the layout structure is not repeated.

The operation and effect of the present invention will now be described.

The primary syngas G1 generated in the reformer flows into the primary syngas inlet 121 of the boiler 120 through the pipe P1 and flows through the primary syngas pipe 125, And is discharged through the discharge portion 122.

The combustion gas discharged from the reformer flows into the combustion gas inflow portion 123 of the boiler 120 through the pipe P6 and is discharged to the combustion gas discharge portion 124 via the combustion gas pipe 126. [

Both the primary synthesis gas and the combustion gas have a temperature of 500 ° C or higher. Therefore, the steam is generated by heating the water filled in the tank portion of the boiler 120 while passing through the primary syngas pipe 125 and the combustion gas pipe 126. The generated water vapor is discharged through the pipe 12 connected to the upper part of the boiler 120 and supplied to the reformer.

The primary syngas (300 ° C. to 350 ° C.) discharged from the primary syngas discharge part 122 is supplied to the conversion reactor 200 through the pipe P 2 to produce hydrogen Thereby generating a syngas synthesis gas G2.

The second synthesis gas G2 (350 DEG C to 450 DEG C) discharged from the conversion reactor 200 flows into the shell side portion inlet of the second heat exchanger 140 through the pipe P3.

The secondary syngas discharged from the outlet of the shell side portion of the second heat exchanger 140 flows into the inlet of the shell side portion of the third heat exchanger 150 through the pipe P4, The secondary syngas discharged at the outlet of the shell side portion is supplied to the PSA apparatus 300 through the pipe P5 and then converted into high purity hydrogen gas by pressure swing adsorption reaction.

The combustion gas (100 ° C to 200 ° C) discharged from the combustion gas discharge portion 124 of the boiler 120 directly flows into the tube side portion of the first heat exchanger 130. The combustion gas (50 ° C to 100 ° C) discharged to the tube side portion outlet of the first heat exchanger 130 is supplied to the inlet of the tube side portion of the fourth heat exchanger 160 through the pipe P7. The combustion gas discharged to the tube side portion outlet of the fourth heat exchanger 160 is discharged to the atmosphere through the pipe P8.

Water (room temperature, about 25 ° C) discharged from the outlet of the water supply unit 500 is supplied to the inlet of the shell side portion of the first heat exchanger 130 through the pipe P9, The water discharged from the side portion outlet is supplied to the inlet of the tube side portion of the second heat exchanger 140 through the pipe P10.

The water discharged from the tube side portion outlet of the second heat exchanger 140 is supplied to the tank portion of the boiler 120 through the pipe P11. The water vapor generated in the tank portion of the boiler 120 is supplied to the reformer via the pipe P12 as described above.

Natural gas (room temperature, about 25 ° C) discharged from the outlet of the natural gas supply unit 400 flows into the inlet of the shell side of the fourth heat exchanger 160 through the pipe P13. The natural gas discharged from the outlet of the shell side portion of the fourth heat exchanger 160 flows into the inlet of the tube side portion of the third heat exchanger 150 through the pipe P14, The natural gas discharged from the sub-outlet is supplied to the reforming reaction section inlet of the reformer through the pipe P15. At this time, the pipe P12 through which water vapor is discharged from the boiler 120 joins the pipe P15 to which the natural gas is supplied. Therefore, natural gas and water vapor are mixed and supplied to the reforming reaction inlet of the reformer.

The following heat exchange is performed in the heat exchangers 130, 140, 150 and 160 by the flow of the fluid (primary syngas, secondary syngas, combustion gas, natural gas, water (steam)).

In the first heat exchanger (130), combustion gas flowing through the tube side portion flows from the water supply portion (500) and heats the water flowing through the shell side portion to heat up the primary side.

In the second heat exchanger (140), water flowing through the tube side portion is secondarily heated by the secondary syngas flowing through the shell side portion, and then supplied to the tank portion of the boiler (120).

In the third heat exchanger (150), the natural gas flowing through the tube side portion is heated by the secondary syngas flowing through the shell side portion and heated to the secondary side, and then supplied to the reformer.

In the fourth heat exchanger (160), the combustion gas flowing through the tube side portion firstly heats natural gas flowing through the shell side portion to raise the temperature. The first heated natural gas is secondarily heated by the secondary syngas as it flows through the tube side portions of the third heat exchanger 150, as described above.

As described above, the water at room temperature supplied from the water supply unit 500 is firstly heated by the combustion gas in the first heat exchanger 130, and the secondary heat is supplied to the second heat exchanger 140 by the second synthesis gas. And is thirdly heated by the high-temperature primary synthesis gas and the combustion gas flowing through the primary synthesis gas pipe 125 and the combustion gas pipe 126 at the boiler 120 to become steam.

The first synthesis gas pipe 125 and the combustion gas pipe 125 are supplied from the boiler 120 to the tank part of the boiler 120 while the first and second heat exchangers 130 and 140 are heated to a sufficient temperature, Even if a smaller amount of heat is absorbed from the heat exchanger 126, it can be vaporized smoothly and converted to water vapor. At this time, the temperature of discharged steam is about 180 ° C, which satisfies the supply condition to the reformer.

The natural gas at room temperature supplied from the natural gas supply unit 400 is firstly heated by the combustion gas in the fourth heat exchanger 160 and the second natural gas is heated by the second synthesis gas at the third heat exchanger 150 And then supplied to the reformer. Therefore, the natural gas can be supplied to the reformer at a sufficiently elevated temperature.

The natural gas and water supplied to the reformer are heated to a sufficient temperature and supplied to the reformer, so that the reforming reaction in the reformer is performed more quickly and actively, thereby increasing the amount of hydrogen production. Further, the amount of natural gas to be supplied to the burner to operate the reformer in a steady state can be reduced, thereby reducing the fuel consumption of the burner. Therefore, the energy efficiency of the entire hydrogen production apparatus is improved.

Meanwhile, the boiler 120 and the first to fourth heat exchangers 130, 140, 150, and 160 are installed inside the case 110 having the heat insulating material, and are insulated from the outside. Therefore, the amount of heat loss is reduced by reducing the amount of heat dissipated to the atmosphere from the boiler 120, the first to fourth heat exchangers 130, 140, 150, and 160, and the plurality of pipes P1 to P15 connecting the heat exchangers 130, .

Further, since the first to fourth heat exchangers 130, 140, 150 and 160 are integrated in the case 110, the length of the pipes connecting the heat exchangers is greatly reduced, and the amount of heat loss through the pipe is greatly reduced. Accordingly, the heat exchange efficiency of the heat exchanger is improved, and the heating performance of natural gas and water by the heat exchanger is greatly improved.

The boiler 120 and the first to fourth heat exchangers 130, 140, 150 and 160 are integrated in the case 110 as described above, Therefore, it is easy to perform maintenance inspection and repair.

The first to fourth heat exchangers 130, 140, 150 and 160 may be arranged in various ways as illustrated in FIG. By stacking a plurality of heat exchangers in the vertical direction as described above, the installation area of the heat exchanger can be greatly reduced. This has the effect of reducing the size of the heat exchanging apparatus 100 and consequently reducing the size of the hydrogen producing apparatus.

Further, by disposing some of the heat exchangers in different columns from the main lamination heat, it is possible to more efficiently perform the arrangement of the connecting pipes between the heat exchangers. For example, when the fourth heat exchanger 160 is separated from the main laminating column and installed on the side of the first heat exchanger 130 as shown in FIG. 2 (a), the first heat exchanger 130 and the fourth heat exchanger 160 can be greatly reduced.

2 (b), when the support frame 180 is used to install the fourth heat exchanger 160 at the same height as the second heat exchanger 140, the position of the fourth heat exchanger 160 The length of the pipe P7 can be reduced while minimizing the increase in the length of the pipe P14 connecting the fourth heat exchanger 160 and the third heat exchanger 150 according to the movement.

2 (c), a second heat exchanger 140 is stacked on the first heat exchanger 130, and a fourth heat exchanger (not shown) is disposed on the side of the first heat exchanger 130 And the third heat exchanger 150 may be stacked on the upper portion of the fourth heat exchanger 160. In this case, all the heat exchangers are located close to each other in the up, down, left, right, and diagonal directions, so that the length of the pipes connected to each other can be reduced.

As described above, the arrangement of the first to fourth heat exchangers 130, 140, 150 and 160 can be variously changed to reduce the length of pipes connecting the first to fourth heat exchangers 130, 140, 150 and 160, and also to simplify the layout of pipes. Therefore, the energy efficiency of the heat exchanger is improved, and the structure is simplified.

When the first to fourth heat exchangers 130, 140, 150 and 160 are formed in a square tube shape, the upper and lower surfaces of the heat exchanger are closely contacted with each other during stacking of the heat exchanger, Can be simplified.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, It is understandable. Accordingly, the true scope of the present invention should be determined by the following claims.

100: heat exchanger 110: case
120: boiler 121: primary syngas inlet
122: Primary syngas discharge part 123: Combustion gas inflow part
124: Combustion gas discharge portion 125: Primary syngas pipe
126: combustion gas pipe 130: first heat exchanger
140: second heat exchanger 150: third heat exchanger
160: fourth heat exchanger 170, 170 ': mounting member
180: support frame 200: conversion reactor
300: PSA apparatus 400: natural gas supply unit
500: water supply part P1 to P15: pipe

Claims (16)

A first heat exchanger 130 installed at a side of the boiler 120 in a boiler 120 and a case 110 installed at one side of the case 110; A second heat exchanger 140, a third heat exchanger 150, and a fourth heat exchanger 160,
Natural gas and water supplied from the natural gas supply unit 400 and the water supply unit 500 provided outside the case 110 are supplied to the reformer installed outside the case 110 and the combustion gas Exchanging heat with the primary syngas and the secondary syngas to supply the reformed gas to the reformer,
The boiler 120 has a primary synthesis gas inlet 121, a primary syngas outlet 122, a combustion gas inlet 123 and a combustion gas outlet 124 formed at a lower portion thereof, The first synthesis gas inlet 121 and the first synthesis gas outlet 122 are connected to the first synthesis gas pipe 125 and the combustion gas inlet 123 and the combustion gas inlet 123 are connected to each other, The gas discharge portion 124 is connected to the combustion gas pipe 126 and the primary syngas pipe 125 and the combustion gas pipe 126 are provided in the inside of the tank portion in the inverted U shape and the primary syngas pipe 125 Characterized in that the water in the tank is heated by the combustion gas flowing through the primary syngas and the combustion gas pipe (126) to generate steam, and the steam is supplied to the reformer through a pipe (P12) connected to the upper part of the tank A heat exchange device for a manufacturing apparatus. The method according to claim 1,
Wherein the case (110) is provided with a heat insulating material on an inner side surface thereof. The method according to claim 1,
Wherein the case (110) is configured such that a part of a side surface thereof can be opened. delete The method according to claim 1,
The primary syngas discharged from the primary syngas discharge portion 122 of the boiler 120 is supplied to the conversion reactor 200 through the pipe P2 and the secondary syngas discharged from the conversion reactor 200 Is supplied to the inlet of the shell side portion of the secondary heat exchanger 140 through the pipe P3 and the secondary syngas discharged from the outlet of the shell side portion of the secondary heat exchanger 140 flows through the pipe P4 The secondary syngas discharged from the shell side portion outlet of the tertiary heat exchanger 150 is supplied to the inlet of the PSA apparatus 300 through the pipe P5 and supplied to the inlet of the shell side portion of the car heat exchanger 150, Wherein the heat exchanger is a heat exchanger. The method of claim 5,
One end of the tubes constituting the tube side portion of the first heat exchanger 130 is directly connected to the combustion gas discharge portion 124 of the boiler 120 so that the combustion gas discharged from the combustion gas discharge portion 124 flows into the first heat exchanger And the combustion gas discharged from the tube side portion outlet of the first heat exchanger 130 is supplied to the tube side inlet of the fourth heat exchanger 160 through the pipe P7, And the combustion gas discharged from the tube side outlet of the fourth heat exchanger (160) is discharged to the atmosphere through the pipe (P8). The method of claim 6,
Wherein the water discharged from the outlet of the water supply part (500) is supplied to the inlet of the shell side part of the first heat exchanger (130) so that the water is firstly heated by the combustion gas. The method of claim 7,
The water discharged from the shell side portion outlet of the first heat exchanger 130 is supplied to the inlet of the tube side portion of the second heat exchanger 140 through the pipe P10 so that water is heated by the second synthesis gas And the water discharged from the tube side portion outlet of the second heat exchanger (140) is supplied to the tank portion of the boiler (120) through the pipe (P11). The method of claim 6,
The natural gas discharged from the outlet of the natural gas supply unit 400 is supplied to the inlet of the shell side portion of the fourth heat exchanger 160 through the pipe P13 so that the natural gas is firstly heated by the combustion gas, The natural gas discharged from the shell side portion outlet of the heat exchanger 160 is supplied to the inlet of the tube side portion of the third heat exchanger 150 through the pipe P14 so that the natural gas is secondarily heated by the second synthesis gas , And the natural gas discharged from the outlet of the tube side portion of the third heat exchanger (150) is supplied to the reformer through the pipe (P15). The method according to claim 1,
Three of the first to fourth heat exchangers 130, 140, 150, and 160 are stacked one on top of the other and one of the other is formed on the bottom plate 111 of the case 110. [ A heat exchange device for a hydrogen producing apparatus. The method according to claim 1,
Three of the first to fourth heat exchangers 130, 140, 150 and 160 are stacked one on top of the other and the other one is formed in another row. The support frame 180 is attached to the bottom plate 111 of the case 110, And the remaining one heat exchanger is installed on the upper part of the support frame (180). The method according to claim 1,
Wherein two of the first to fourth heat exchangers (130, 140, 150, and 160) are stacked one on top of the other and the other two are stacked on top of each other. The method according to claim 1,
The first to fourth heat exchangers (130, 140, 150, 160) are formed in a rectangular tube shape so that the lower surface of the upper side heat exchanger and the upper surface of the lower side heat exchanger Heat exchanger. The method according to any one of claims 10 to 12,
The first to fourth heat exchangers 130, 140, 150 and 160 are fixed to each other via a mounting member 170. The mounting member 170 includes an upper mounting plate 171 fixed to a lower portion of the upper heat exchanger, And a bolt (173) penetratingly connected to both ends of the upper mounting plate (171) and the lower mounting plate (172), characterized in that the lower mounting plate (172) Device. 15. The method of claim 14,
Wherein a support block (174) is interposed between the upper mounting plate (171) and the lower mounting plate (172) to secure a distance and a space between the upper heat exchanger and the lower heat exchanger. 14. The method of claim 13,
The first to fourth heat exchangers 130, 140, 150 and 160 are fixed to each other via a mounting member 170 ', and the mounting member 170' includes an upper mounting flange 171 'formed on both lower sides of the upper heat exchanger , A lower mounting flange 172 'formed on both upper end sides of the lower heat exchanger and a bolt 173' penetrating the upper mounting flange 171 'and the lower mounting flange 172' A heat exchange device for a manufacturing apparatus.

KR1020150059455A 2015-04-28 2015-04-28 Heat exchanging device of hydrogen producing apparatus KR101747516B1 (en)

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Publication number Priority date Publication date Assignee Title
WO2023121111A1 (en) * 2021-12-23 2023-06-29 경남큐에스에프 주식회사 Complete energy consumption-type lng convergence utilization system and method

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JP2002212566A (en) 2001-01-17 2002-07-31 Nippon Steel Corp Coke dry quenching apparatus and quenching method using the same
JP2006096622A (en) * 2004-09-30 2006-04-13 Mitsubishi Heavy Ind Ltd Hydrogen production system
JP2008538097A (en) * 2005-03-29 2008-10-09 テキサコ ディベラップメント コーポレイション Method and apparatus for a heat integrated hydrogen generation system
JP2010254544A (en) 2009-03-30 2010-11-11 Tokyo Gas Co Ltd Hydrogen separation type hydrogen production system having carbon dioxide separation recovery device attached thereto
JP2014122722A (en) * 2012-12-20 2014-07-03 Mitsubishi Electric Corp Outdoor unit of air conditioner and manufacturing method of the outdoor unit of the air conditioner

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002212566A (en) 2001-01-17 2002-07-31 Nippon Steel Corp Coke dry quenching apparatus and quenching method using the same
JP2006096622A (en) * 2004-09-30 2006-04-13 Mitsubishi Heavy Ind Ltd Hydrogen production system
JP2008538097A (en) * 2005-03-29 2008-10-09 テキサコ ディベラップメント コーポレイション Method and apparatus for a heat integrated hydrogen generation system
JP2010254544A (en) 2009-03-30 2010-11-11 Tokyo Gas Co Ltd Hydrogen separation type hydrogen production system having carbon dioxide separation recovery device attached thereto
JP2014122722A (en) * 2012-12-20 2014-07-03 Mitsubishi Electric Corp Outdoor unit of air conditioner and manufacturing method of the outdoor unit of the air conditioner

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023121111A1 (en) * 2021-12-23 2023-06-29 경남큐에스에프 주식회사 Complete energy consumption-type lng convergence utilization system and method

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