KR20190111539A - Apparatus for water gas shift reaction - Google Patents

Abstract

The present invention relates to an apparatus for water gas conversion reaction. In an embodiment, the apparatus for water gas conversion reaction comprises: a reactor having a heat exchanger comprising a catalyst layer for converting water gas and generating a gas composition comprising carbon dioxide and hydrogen by inflow of synthetic gas containing carbon monoxide from a gas inlet line; and a water spraying line provided at a lower part of the reactor and equipped with a plurality of spray nozzles for injecting water into a lower part of the heat exchanger, wherein the synthetic gas generates a first gas mixture by contacting with the sprayed water and the first gas mixture is introduced into the lower part of the heat exchanger and heated by heat exchange and catalyst reaction, thereby producing the gas composition comprising carbon dioxide and hydrogen. According to the present invention, by effectively lowering a temperature of the reactor through heat exchange, water gas conversion reaction efficiency is excellent.

Description

Water gas shift reactor {APPARATUS FOR WATER GAS SHIFT REACTION}

The present invention relates to a water gas shift reactor.

An integrated gasification fuel cell (IGFC) system is a system for generating electricity by using a synthesis gas provided from a gasifier as a fuel of a fuel cell. It is a technology that pretreats synthetic gas produced by coal gasification to make high purity hydrogen or methane (CH ₄ ) and uses it as fuel of fuel cell. It is one of the next generation power generation systems combined with efficiency.

On the other hand, in the case of a hydrogen fuel cell type, it is necessary to convert the purified syngas into hydrogen through a water gas shift reactor. The reaction formula of the water gas shift reaction (CO-Shift) occurring in the water gas shift reactor for converting carbon monoxide in the synthesis gas to hydrogen is shown in Scheme 1 below. For effective hydrogen conversion, heat must be removed or steam added in excess of stoichiometric ratio in accordance with Le-Charlestrie's law:

Scheme 1

_{CO + H 2 O ↔ CO 2} + H 2 - 41.2KJ / mol

Reaction Scheme 1 may increase the reaction conversion rate by removing heat of the reactor as an exothermic reaction or by adding an excessive amount of water (steam) in the reactants. Therefore, a technology for lowering the temperature of the reactor and generating steam from the hot gas after the reaction and reusing it has been developed and commercialized.

Figure 1 shows a general water gas conversion reactor. Referring to FIG. 1, the water gas shift reaction apparatus includes a separator (a), a first stage reactor (c), a two stage reactor (d), a separator (f), and a heat exchanger (b, e, c '). ).

The synthesis gas flowing into the CO-Shift reaction process of the water gas shift reactor is in contact with the hot water and countercurrent in the saturator (a), the temperature of the water decreases and the synthesis gas evaporates from the hot water. Mixed with one water vapor. Generally, the temperature of the syngas flowing into the separator (a) is about 40 ° C., and the introduced dry syngas is a high temperature circulating water of about 250 ° C., and when saturated in contact with countercurrent, steam is saturated. In this process, the hot water is cooled and the cooled water is heated to a high temperature by direct contact with the hot gas after the CO-Shift reaction process in a desaturator (f). Recycle to a).

Sechyu the synthesis gas discharged from the concentrator (a) is included in the steam of about dry gas (dry gas) based on about ^{0.85kg / Nm 3 (1.05Nm 3 Water} / Nm 3 Gas) is discharged from the sechyu concentrator. If the concentration of carbon monoxide (CO) in the synthesis gas is 45% by volume, for a reaction of about 90% conversion, a total of 1.47 mol steam / mol gas is required at a reaction temperature of 430 ° C (0.41 mol of steam for reaction). , Steam for equilibrium 1.06 mol).

The separator / de-sectorator circulating water, which discharges heat from the separator (a) to the synthesis gas, is discharged to about 190 ° C. and heated again in the de-sector (f), and the first and second reactors The heat is reheated by heat exchange in the heat exchanger, and is reintroduced into the top of the separator (a) at a temperature of 250 ° C.

Figure 2 shows a typical water gas conversion reactor. As described above, the stoichiometrically controlled syngas is introduced into a countercurrent cooled water gas reactor (Countercurrent Gas Cooled Reactor) as shown in FIG. 2.

Referring to FIG. 2, the synthesis gas introduced into the reactor undergoes a CO-Shift reaction while passing through the catalyst bed, thereby increasing the temperature of the gas. In one embodiment, the inside of the reactor, the shell and tube (Shell and Tube) type heat exchanger structure as shown in FIG. In the heat exchanger, a tube is provided between the heat exchange medium in the form of a shell, and a catalyst layer is formed by filling a catalyst for the CO-Shift reaction in the space between the shell and the tube. The syngas exchanges heat with the high temperature syngas moving the catalyst layer formed outside the tube while moving inside the tube in a direction opposite to the high temperature syngas flow in the catalyst before entering the catalyst layer.

Figure 3 shows the temperature profile (profile) inside the reactor for water gas conversion. Referring to FIG. 3, the synthesis gas of about 230 ° C. introduced into the tube of the reactor (first reactor) through the heat exchange is preheated to about 380 ° C. before entering the catalyst bed. When the preheated syngas passes through the catalyst bed, the temperature of the syngas rapidly increases with the reaction. Part of the reaction heat generated at this time is used to heat and heat the syngas before the reaction inside the tube. The temperature of the catalyst bed rises to at least 550 ° C. In addition, the syngas is finally discharged from the reactor (stage 1 reactor) at a temperature of about 410 ℃. On the other hand, since the temperature inside the reactor exchanges heat with the inlet syngas, it can be seen that the temperature of each part is different.

The syngas discharged from the first stage reactor (c) is cooled to a temperature suitable for introduction into the heat recovery and the second stage reactor (d) through a heat exchanger. As described above, since the CO-Shift reaction is an exothermic reaction, the conversion rate is increased when the reactor temperature is low. In particular, since about 90% of the total reaction occurs in the first stage reactor (c), since the gas temperature due to the heat of reaction of the second stage reactor (d) is also relatively low, the two stage reactor is the same as the first stage reactor (c). No countercurrent gas cooled reactor is used. The reaction temperature of the two-stage reactor is about 360-380 degrees, but this is a variable number. The overall reaction efficiency of the reactor is around 90% and this conversion rate is very fluid depending on the temperature and the amount of steam.

Typically, water-gas shift reactors use multiple reactors, such as Shell Low Steam Shift, maintain a constant temperature, such as an isothermal reactor, or use a separator and desectator ( Saturator and Desaturator (Saturator and Desaturator) A method of producing steam by contacting hot syngas with water, such as a reactor, or using a heat exchanger integrated reactor.

The prior art had the disadvantage that the reactor system was complex and expensive. In particular, when converting coal gasification syngas to hydrogen, a large amount of steam is required to convert the CO ratio to about 60% hydrogen. In addition, there is a disadvantage that the CO-Shift reaction rate is lowered due to the high heat generated by the reaction.

Background art of the present invention is disclosed in Republic of Korea Patent Publication No. 10-1103594 (2012.01.02, the name of the invention: a multi-stage fluidized bed water gas reactor using gasification synthesis gas and a hydrogen production method using the same) and the like.

One object of the present invention is to provide a water gas shift reaction apparatus excellent in water gas shift reaction efficiency.

Another object of the present invention is to provide a water gas shift reaction apparatus capable of simplifying and miniaturizing the apparatus.

Still another object of the present invention is to provide a water gas conversion reaction apparatus capable of reducing steam consumption and power consumption for a conversion reaction, and having excellent economic efficiency.

One aspect of the present invention relates to a water gas shift reactor. In one embodiment, the water gas shift reaction apparatus includes a heat exchanger including a catalyst layer for water gas conversion, and a synthesis gas including carbon monoxide is introduced from a gas inlet line to generate a gas composition including carbon dioxide and hydrogen. ; And a water spray line provided at a lower portion of the reactor and having a plurality of spray nozzles for injecting water into the heat exchanger, wherein the syngas is in contact with the sprayed water to generate a first gas mixture. The first gas mixture is introduced into the lower part of the heat exchanger and heated through heat exchange and catalysis to produce a gas composition including carbon dioxide and hydrogen.

In one embodiment, the water spray line further includes a gas header formed along the spray nozzle, and the gas header is connected to the gas inlet line to introduce the syngas into the lower portion of the heat exchanger. You can.

In one embodiment the heat exchanger includes a shell heat exchange member; A plurality of tubes provided inside the heat exchange member; And a catalyst layer formed by filling a catalyst in a space between the heat exchange member and the tube, wherein the lower portion of the tube is opened to introduce a first gas mixture, and the first gas mixture moves to an upper portion of the tube. The heated first gas mixture inside the catalyst layer is heated through heat exchange, and the heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, and is heated by a catalytic reaction to include carbon dioxide and hydrogen. Gas compositions can be produced.

In one embodiment, the heat exchanger includes a plate heat exchange member having a plurality of spaced apart plates; And a catalyst layer formed by filling a catalyst in the spaced space of the heat exchange member, wherein the first gas mixture flows into the lower portion of the heat exchange member and moves upwards, and moves the heated first gas to move the catalyst layer. Heated through a mixture and heat exchange, the heated first gas mixture may be introduced into the upper portion of the catalyst layer and moved to the lower side, and heated by a catalytic reaction to generate a gas composition including carbon dioxide and hydrogen.

In one embodiment, the temperature of the first gas mixture flowing into the catalyst layer may be 200 to 350 ° C.

In one embodiment, the temperature of the catalyst layer may be 270 ~ 450 ℃.

In one embodiment, the bottom of the reactor is further provided with a water separator, it is possible to remove the water that is not in contact with the syngas from the bottom of the heat exchanger.

In one embodiment, the gas composition may be discharged to the outside through a gas discharge line provided under the catalyst layer of the heat exchanger.

In one embodiment, the water gas shift reactor is provided in the water injection line, the flow rate control valve for controlling the injection amount of the water; A flow rate meter provided in the gas inlet line for measuring a flow rate of the syngas; And a thermometer provided at an upper portion of the heat exchanger. It may further comprise one or more of.

In one embodiment, the first gas mixture introduced into the lower portion of the heat exchanger may include water and carbon monoxide in a molar ratio of 1: 1 to 3: 1.

When the water gas shift reaction apparatus according to the present invention is applied, the efficiency of the water gas shift reaction is excellent by effectively lowering the temperature of the reactor through heat exchange, and the reaction apparatus can be simplified and downsized, and the reaction is performed using heat generated in the reactor. By generating the molten steam, it is possible to improve the reaction rate and minimize the steam consumption and power consumption.

Figure 1 shows a general water gas conversion reactor.
Figure 2 shows a typical water gas conversion reactor.
Figure 3 shows the temperature profile inside the reactor for water gas conversion.
Figure 4 shows a water gas conversion reaction apparatus according to an embodiment of the present invention.
Figure 5 shows a water gas conversion reactor according to another embodiment of the present invention.
Figure 6 is a graph showing the correlation between the reactor internal temperature, the content of steam entering the reactor and the conversion rate.

In the following description of the present invention, when it is determined that detailed descriptions of related well-known technologies or configurations may unnecessarily obscure the subject matter of the present invention, the detailed description will be omitted.

The terms to be described below are terms defined in consideration of functions in the present invention, and may be changed according to intentions or customs of users or operators, and the definitions should be made based on the contents throughout the present specification for describing the present invention.

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

Water Gas Conversion Reactor

One aspect of the present invention relates to a water gas shift reactor. Figure 4 shows a water gas conversion reaction apparatus according to an embodiment of the present invention. Referring to FIG. 4, the water gas shift reaction apparatus 1000 includes a heat exchanger 200 including a catalyst layer for converting water gas, and a synthesis gas containing carbon monoxide is introduced from the gas inlet line 10 to provide carbon dioxide. And a reactor 100 generating a gas composition including hydrogen; And a water spray line 320 provided at a lower portion of the reactor 100 and having a plurality of spray nozzles 300 for injecting water into the lower portion of the heat exchanger 200. In contact with water to produce a first gas mixture, the first gas mixture is introduced into the lower portion of the heat exchanger 200 and heated through heat exchange and catalysis, and includes carbon dioxide (CO ₂ ) and hydrogen (H- ₂ ). To produce a gas composition.

In one embodiment, the temperature of the first gas mixture flowing into the lower portion of the heat exchanger may be 200 to 350 ° C. Gas compositions in the above range can be easily produced.

In one embodiment, the first gas mixture flowing into the lower portion of the heat exchanger is water and carbon monoxide. 1: 1 to 3: molar ratio May be included. When included in the molar ratio, the production efficiency of the gas composition from the first gas mixture may be excellent. The molar ratio of water and carbon monoxide can be adjusted according to the target conversion rate of carbon monoxide to carbon dioxide and the composition of carbon monoxide and carbon dioxide of the first gas mixture.

The heat exchanger may comprise a shell and tube heat exchanger or a plate heat exchanger.

For example, it may include a shell and tube heat exchanger. In one embodiment the heat exchanger includes a shell heat exchange member; A plurality of tubes provided inside the heat exchange member; And a catalyst layer formed by filling a catalyst in a space between the heat exchange member and the tube, wherein the lower portion of the tube is opened to introduce a first gas mixture, and the first gas mixture moves to an upper portion of the tube. The heated first gas mixture inside the catalyst layer is heated through heat exchange, and the heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, and is heated by a catalytic reaction to include carbon dioxide and hydrogen. Gas compositions can be produced.

In one embodiment, the water gas conversion catalyst may include a high temperature shift (HTS) catalyst. For example, a catalyst containing chromium oxide (CrO ₃ ) and iron oxide (Fe ₃ O ₄ ) can be used. The catalyst may be formed to be porous to allow the first gas mixture to move.

In an embodiment, the outer wall of the reactor 100 may have a diaphragm formed at an upper portion and a lower portion of the heat exchanger 200. When the diaphragm is formed, the first gas mixture may flow into the lower portion of the tube of the heat exchanger 200 only.

In specific embodiments, the water may be pure water. The water sprayed through the spray nozzle is in contact with the lower end of the high temperature heat exchanger and part of the water is vaporized, but most of the water may be included in the high temperature synthesis gas in the form of fine droplets and introduced into the heat exchanger.

The first gas mixture is heated while exchanging heat with the heated first gas mixture in the catalyst layer, and the water included in the first gas mixture may be converted into steam. As the first gas mixture moves to the upper portion of the tube, the first gas mixture is further heated through heat exchange with the first gas mixture inside the catalyst layer, so that the temperature of the syngas increases further and steam contained in the syngas in the process is supersaturated steam. Can be

In one embodiment, the temperature of the first gas mixture flowing into the upper portion of the catalyst layer may be 200 to 350 ° C. For example, about 320 ° C. At this temperature condition, a gas composition comprising hydrogen and carbon dioxide can be readily produced in the presence of a catalyst.

The first gas mixture introduced into the catalyst layer moves from top to bottom, and the carbon monoxide in the first gas mixture is reacted with the steam to generate a gas composition including carbon dioxide and hydrogen through a catalytic reaction. The reaction heat is generated in the reaction process, the temperature of the gas composition is raised to about 550 ℃, but the reaction heat is discharged through the heat exchanger, the temperature of the catalyst layer may be 270 ~ 450 ℃. Gas compositions in the above range can be easily produced.

In one embodiment, the bottom of the reactor is further provided with a water separator (not shown), it is possible to remove the water that is not in contact with the syngas in the lower portion of the heat exchanger.

In one embodiment, water that is not entrained with syngas in the water sprayed from the spray nozzles 300 and 301 is collected into drain tanks 400 and 401 formed at the bottom of the reactors 100 and 101, thereby allowing the reactor. Can be discharged to the outside. In one embodiment, the amount of water discharged out of the reactor can be calculated to determine the injection amount of water to be introduced into the reactor.

Figure 5 shows a water gas conversion reactor according to another embodiment of the present invention. Referring to FIG. 5, the water spray line 321 may further include a gas header 330 formed along the spray nozzle 301. The gas header 330 may be connected to the gas inflow line 11 to introduce the synthesis gas into the lower portion of the heat exchanger 210.

Other examples may include plate heat exchangers. In one embodiment, the heat exchanger includes a plate heat exchange member having a plurality of spaced apart plates; And a catalyst layer formed by filling a catalyst in the spaced space of the heat exchange member. The first gas mixture flows into the lower portion of the heat exchange member and moves upwards, and is heated through heat exchange with the heated first gas mixture moving the catalyst layer, and the heated first gas mixture is moved to the upper portion of the catalyst layer. As it is introduced and moved downwards, it is heated by a catalytic reaction to produce a gas composition including carbon dioxide and hydrogen.

In specific embodiments, the water may be pure water. The water sprayed through the spray nozzle is in contact with the lower end of the high temperature heat exchanger and part of the water is vaporized, but most of the water may be included in the high temperature synthesis gas in the form of fine droplets and introduced into the heat exchanger.

In one embodiment, the first gas mixture is introduced into the lower portion of the heat exchange member, and is heated by heat exchange with the heated first gas mixture moving the catalyst layer, and the water in the first gas mixture may be converted into steam. . The first gas mixture is continuously heated while moving from the lower portion of the heat exchange member to the upper portion, the temperature of the syngas in the first gas mixture is further increased, and the steam may be supersaturated steam.

In one embodiment, the temperature of the first gas mixture flowing into the upper portion of the catalyst layer may be 300 to 350 ° C. For example, it may be 320 ℃. At this temperature condition, a gas composition comprising hydrogen and carbon dioxide can be readily produced in the presence of a catalyst.

The first gas mixture introduced into the catalyst layer moves from top to bottom, and the carbon monoxide in the first gas mixture is reacted with the steam to generate a gas composition including carbon dioxide and hydrogen through a catalytic reaction. The reaction heat is generated in the reaction process, the temperature of the gas composition is raised to about 550 ℃, but the reaction heat is discharged through the heat exchanger, the temperature of the catalyst layer may be 350 ~ 450 ℃. Gas compositions in the above range can be easily produced.

In one embodiment, the bottom of the reactor is further provided with a water separator (not shown), it is possible to remove the water that is not in contact with the syngas in the lower portion of the heat exchanger.

4 and 5, the gas composition may be discharged out of the reactor through gas discharge lines 20 and 21 provided under the heat exchanger. For example, the gas composition may be discharged out of the reactor through gas discharge lines 20 and 21 provided under the catalyst layer of the heat exchanger.

4 and 5, the water gas shift reaction apparatus (1000, 2000) is provided in the water injection line (320, 321), flow control valves (310, 311) for controlling the injection amount of the water; Flow measuring meters (14, 15) provided in gas inlet lines (10, 11) for measuring the flow rate of the syngas; And thermometers 12 and 13 provided on the heat exchangers 200 and 210 to measure temperature. It may further comprise one or more of.

In one embodiment, the amount of pure water introduced may be controlled through a synthesis gas inflow value measured through a temperature and flow meter at the top of the heat exchanger (or the top of the reactor) measured using the thermometer. For example, the injection amount of the water flowing through the gas injection line, based on the temperature of the top of the heat exchanger and the synthesis gas inflow amount, the flow control valve so that the water in contact with the synthesis gas in the first gas mixture is maintained in a supersaturated state Can be adjusted using.

When the water gas shift reaction apparatus according to the present invention is applied, the efficiency of the water gas shift reaction is excellent by effectively lowering the temperature of the reactor through heat exchange, and the reaction apparatus can be simplified and downsized, and the reaction is performed using heat generated in the reactor. By generating the molten steam, it is possible to improve the reaction rate and minimize the steam consumption and power consumption.

The complex process consisting of the existing separator / desectator, syngas pipe, and circulation pump pipe is changed to simple water spray system, which greatly reduces investment and facility operating cost, and saves electricity cost by not using the circulation pump. And, since the reactor temperature is lowered, the reaction efficiency may be excellent.

Hereinafter, the configuration and operation of the present invention through the preferred embodiment of the present invention will be described in more detail. However, this is presented as a preferred example of the present invention and in no sense can be construed as limiting the present invention.

Example  One

A water gas shift reaction apparatus as shown in FIG. 4 was prepared. Specifically, the reactor 100 is provided with a heat exchanger 200 comprising a catalyst layer for water gas conversion; And a water spray line 320 provided at a lower portion of the reactor 100 and having a plurality of spray nozzles 300 for spraying water to the lower portion of the heat exchanger 200. The heat exchanger includes a shell. Heat exchange member of the form; A plurality of tubes provided inside the heat exchange member; And a catalyst layer formed by filling a catalyst in a space between the heat exchange member and the tube.

In addition, a lower portion of the reactor 100 is provided with a water separator for removing water that is not in contact with the syngas from the heat exchanger 200, the water spray line 320 flow control valve for controlling the injection amount of the water (310), the gas inlet line (10) was provided with a flow meter (14) for measuring the flow rate of the incoming synthesis gas, and a thermometer (12) for measuring the temperature on top of the heat exchanger. .

Syngas introduced into the reactor contacted the injected water to produce a first gas mixture of about 280 ° C. Water and carbon monoxide in the first gas mixture were included in a molar ratio of 1: 1 to 3: 1.

The first gas mixture flowed into the lower portion of the open tube and moved upwards through heat exchange with the heated first gas mixture inside the catalyst bed. At this time, the water in the first gas mixture, introduced into the lower portion of the tube was converted to steam, heated while moving to the upper portion of the tube was converted to supersaturated steam. The temperature of the first gas mixture flowing into the upper portion of the catalyst layer was heated to about 320 ° C.

The heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, thereby being heated by a catalytic reaction to produce a gas composition including carbon dioxide and hydrogen. The temperature of the gas composition was raised to about 550 ° C., and the heat of reaction was released during the heat exchange with the first gas mixture moving inside the tube, so that the temperature of the catalyst layer was maintained at about 380 ° C.

In addition, water that is not entrained with the synthesis gas in the water sprayed from the spray nozzle 300 is collected into a drain tank 400 formed under the reactor 100 and discharged outside the reactor.

Example  2

A water gas shift reaction apparatus as shown in FIG. 5 was prepared. Specifically, the reactor 101 is provided with a heat exchanger 210 comprising a catalyst layer for water gas conversion; And a water spray line 321 provided at a lower portion of the reactor 101 and having a plurality of spray nozzles 301 for injecting water into the lower portion of the heat exchanger 210. Heat exchange member in the form of a plate (plate) spaced apart dog; And a catalyst layer formed by filling a catalyst in spaced spaces of the heat exchanging member.

The water spray line 321 has a gas header 330 formed along the spray nozzle 301, and the gas header is connected to the gas inlet line 11 to transfer the syngas to the bottom of the heat exchanger. Inflow.

In addition, the lower portion of the reactor 101 is provided with a water separator for removing the water that is not in contact with the syngas from the heat exchanger 210, the water spray line 321 flow control valve for controlling the injection amount of the water 311, the gas inlet line 11 has a flow meter 15 for measuring the flow rate of the incoming synthesis gas, and a thermometer 13 for measuring the temperature at the top of the heat exchanger. .

Syngas introduced into the reactor contacted the injected water to produce a first gas mixture of about 280 ° C. Water and carbon monoxide in the first gas mixture were included in a molar ratio of 1: 1 to 3: 1.

The first gas mixture flows into the lower portion of the plate heat exchange member of the heat exchanger 210 and is heated through heat exchange with the heated first gas mixture inside the catalyst layer while moving upward. At this time, the water in the first gas mixture introduced into the lower portion of the heat exchange member was converted to steam, and heated while moving to the upper portion of the heat exchange member to convert the steam into supersaturated steam. The temperature of the first gas mixture flowing into the upper portion of the catalyst layer was heated to about 320 ° C.

The heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, thereby being heated by a catalytic reaction to produce a gas composition including carbon dioxide and hydrogen. The temperature of the gas composition was increased to about 550 ° C., and the heat of reaction was released during the heat exchange with the first gas mixture moving inside the heat exchange member. Thus, the temperature of the catalyst layer was maintained at about 380 ° C.

In addition, the water that is not entrained with the synthesis gas in the water sprayed from the spray nozzle 301 is collected into a drain tank 401 formed under the reactor 101 and discharged to the outside of the reactor.

When the water gas conversion reaction apparatus according to Examples 1 to 2 was applied, the conversion rate was measured to 90%, and the conversion efficiency was superior to that of the comparative example (conversion rate 85%) using the reactor as shown in FIG. In the case of the investment cost of Example 1, it takes 80% of the cost compared to the comparative example, it can be seen that the economic efficiency is excellent.

6 is a graph showing the correlation between the reactor internal temperature, the content of steam (water) introduced into the reactor, and the conversion rate. Referring to FIG. 6, the lower the temperature of the reactor, the better the carbon monoxide conversion.

On the other hand, the prior art was to reduce the energy of the heat exchanger through the heat exchange in the inlet gas and the reactor, and to use the hot gas discharged from the reactor for the humidification of the inlet gas to save energy and increase the reaction efficiency.

However, the prior art, including the separator and the de-settler, the device is complicated and expensive to maintain, additional power required to drive the circulation pump to circulate the water, hot gas is introduced into the reactor It was difficult to effectively lower the temperature of the reactor even when the internal heat exchanger was applied.

On the other hand, in the present invention, the complex process consisting of the existing separator / de-sectator, syngas pipe, and circulation pump pipe is changed to a simple water spray system, thereby reducing the investment and facility operating cost, and does not use the circulation pump. The power cost can be reduced, and the reaction temperature can be excellent because the reactor temperature is lowered.

Simple modifications or changes of the present invention can be easily carried out by those skilled in the art, and all such modifications or changes can be seen to be included in the scope of the present invention.

10, 11: gas inlet line 12, 13: thermometer
14, 15: flow meter 20, 21: gas discharge line
100, 101: reactor 200, 210: heat exchanger
300, 301: spray nozzles 310, 311: flow control valve
320, 321: flow control valve 330: gas header
400, 401: drain tank
1000, 2000: water gas shift reactor

Claims (10)

A reactor having a heat exchanger including a catalyst layer for converting water gas, wherein a synthesis gas including carbon monoxide is introduced from a gas inlet line to generate a gas composition including carbon dioxide and hydrogen; And
And a water spray line provided at a lower portion of the reactor and having a plurality of spray nozzles for injecting water into the lower portion of the heat exchanger.
The syngas is in contact with the injected water to produce a first gas mixture,
The first gas mixture is introduced into the lower portion of the heat exchanger is heated by heat exchange and catalytic reaction, water gas conversion reactor characterized in that to produce a gas composition containing carbon dioxide and hydrogen.
The water spraying line of claim 1, wherein the water spray line further comprises a gas header formed along the spray nozzle,
The gas header is connected to the gas inlet line, water gas conversion reaction apparatus, characterized in that for introducing the synthesis gas to the lower portion of the heat exchanger.
The heat exchanger of claim 1, wherein the heat exchanger comprises: a shell heat exchange member;
A plurality of tubes provided inside the heat exchange member; And
And a catalyst layer formed by filling a catalyst in the space between the heat exchange member and the tube.
The lower part of the tube is opened to introduce the first gas mixture,
The first gas mixture is heated through heat exchange with the heated first gas mixture inside the catalyst layer while moving to the top of the tube,
The heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, and is heated by a catalytic reaction to generate a gas composition including carbon dioxide and hydrogen.
The heat exchanger of claim 1, wherein the heat exchanger comprises: a heat exchange member having a plate shape having a plurality of spaced apart from each other; And a catalyst layer formed by filling a catalyst in the spaced space of the heat exchange member.
The first gas mixture is heated through heat exchange with the heated first gas mixture moving the catalyst layer while flowing into the lower portion of the heat exchange member and moving upward,
The heated first gas mixture flows into the upper portion of the catalyst layer and moves downward, and is heated by a catalytic reaction to generate a gas composition including carbon dioxide and hydrogen.
The water gas shift reactor according to claim 1, wherein the temperature of the catalyst layer is 270 to 450 ° C.
The water gas shift reactor according to any one of claims 3 to 4, wherein the temperature of the first gas mixture flowing into the catalyst layer is 200 to 350 ° C.
The water gas shift reactor according to claim 1, further comprising a water separator at the bottom of the reactor to remove water that is not in contact with the syngas from the bottom of the heat exchanger.
The water gas shift reactor according to claim 1, wherein the gas composition is discharged to the outside through a gas discharge line provided under the catalyst layer of the heat exchanger.
According to claim 1, wherein the water gas conversion reactor,
A flow rate control valve provided in the water spray line to control the injection amount of the water;
A flow rate meter provided in the gas inlet line for measuring a flow rate of the syngas; And
A thermometer provided at an upper portion of the heat exchanger; Water gas conversion reactor further comprises one or more of.
The water gas shift reactor according to claim 1, wherein the first gas mixture flowing into the heat exchanger comprises water and carbon monoxide in a molar ratio of 1: 1 to 3: 1.

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