KR101494796B1 - System and method for transforming synthesis gas - Google Patents

Abstract

The present invention relates to a system and a method for transforming synthesis gas that can control, without restriction, the composition of gas generated in the transforming reaction of water gas while increasing thermal efficiency. According to an embodiment of the present invention, the system for transforming synthesis gas comprises: a catalytic reactor for changing the composition ratio of CO and H_2 of synthesis gas by making the synthesis gas including CO and H_2 react with steam generated by a steam generator; a steam control valve for controlling the flow of steam coming into the catalytic reactor; a heat exchanger for making generated gas generated by reaction in the catalytic reactor exchange heat with the synthesis gas; a heater for heating the synthesis gas discharged after exchanging heat with the generated gas in the heat exchanger; a cooler for cooling the generated gas discharged after exchanging heat with the synthesis gas in the heat exchanger; a separator for liquefying and separating steam contained in the generated gas cooled in the cooler; a control valve for adjusting the flow of the synthesis gas coming into the heat exchanger; and a control part for controlling the calorific value of the heater, the openness of the control valve and the openness of the steam control valve.

Description

TECHNICAL FIELD The present invention relates to a system and a method for converting a syngas,

The present invention relates to a syngas conversion system and method.

Gasification is a technology that converts carbon-based fuel into oxidizing agent such as oxygen, steam, etc., and converts it into syngas mainly composed of CO and H _{2. The} converted syngas can be further refined and converted into crude oil Can be used as a new raw material source.

Among these technologies, the most widely applied technology is a coal gasification-based power generation method, in which a syngas obtained through gasification is burned to drive a gas turbine, a steam is taken using a high-temperature combustion gas to be discharged, (IGCC, Integrated Gasification Combined Cycle).

Another application field of synthesis gas is the technology field of manufacturing liquid fuel or chemical raw materials by synthesizing CO and H ₂ under appropriate catalyst. Synthesis natural gas (SNG), hydrogen (H ₂ ), ammonia (NH ₃ ), and natural gas (LNG) are produced through the production of methanol, DME and Fisher- And the like.

The main reaction schemes for obtaining such raw materials from syngas are as follows.

- SNG: CO + 3H ₂ → CH ₄ + H ₂ O (using Ni catalyst, 20 to 30 atm, 300 to 700 ° C)

- Methanol: CO + 2H ₂ → CH ₃ OH (using Cu / ZnO catalyst, 30 ~ 80 atm, 200 ~ 300 ℃)

- DME: 3CO + 3H ₂ → CH ₃ OCH ₃ + CO ₂ (using Cu / ZnO / γ-Al ₂ O 3 catalyst, 50 to 60 atm, 240 to 270 ° C)

- Fisher-Tropsh: nCO + 2nH ₂ → (-CH ₂ -) n + nH ₂ O (using Co and Fe catalyst, 10 to 50 atm, 180 to 250 ° C or 330 to 550 ° C)

As described above, in order to produce the raw material from the gasified synthesis gas, the composition ratio of CO and H ₂ should be 1: 1 to 1: 3. That is, the proportion of hydrogen should be higher than the proportion of carbon monoxide. However, the CO and H ₂ components of the syngas produced in the gasifier are in the range of about 1: 0.5 to 1: 1, and since the hydrogen has a lower ratio, the proportion of hydrogen must be increased. For this purpose, a water gas conversion reaction is used. This water gas conversion reaction is basically a reaction using a catalyst, and the reaction formula is as follows.

- Water gas conversion reaction: CO + H ₂ O ↔CO ₂ + H ₂ ΔH = - 41.2 kJ / mol

Meanwhile, the conventional technologies disclosed in the patent documents are based on the above-mentioned conventional technologies, in which when the composition of the synthesis gas is changed using such a water gas conversion reaction, the synthesis gas component is controlled by a valve for each position of the catalyst reactor (Patent Document 1) (Patent Document 2), the composition ratio of the synthesis gas is controlled as desired.

However, the conventional technology according to Patent Document 1 has a problem that the range in which the synthesis gas ratio can be controlled can be limited depending on the quantity of the valves installed in the catalytic reactor. The conventional technology according to Patent Document 2, There is a disadvantage in that it is necessary to separately supply the auxiliary fuel by injecting the auxiliary fuel into the latter stage of the conversion process, which is not preferable in terms of energy efficiency.

In the prior arts including Patent Documents 1 and 2, since the reaction heat is discarded by cooling the inside of the reactor or by cooling the gas produced after the reaction without using the reaction heat generated in the catalytic reactor, There is a disadvantage that it is not high.

Korean Patent No. 10-0969654 Korea Patent Publication No. 2013-0015808

Embodiments of the present invention have been made in view of the problems of the prior art as described above, and the present invention has been made in view of the above problems, and it is an object of the present invention to control the composition of a gas produced by a water gas conversion reaction So that the synthesis gas can be regulated at a desired ratio without restriction.

According to an aspect of the present invention, there is provided a catalytic reactor for reacting a synthesis gas containing CO and H ₂ with steam generated by a steam generator to change a composition ratio of CO and H ₂ of the synthesis gas; A steam control valve for controlling a flow rate of steam flowing into the catalytic reactor; A heat exchanger for heat-exchanging the syngas produced by the reaction in the catalytic reactor; A heater for heating the syngas discharged from the heat exchanger after heat exchange with the product gas; A cooler for cooling the produced gas discharged from the heat exchanger after heat exchange with the syngas; A separator for liquefying and separating steam contained in the product gas cooled in the cooler; A syngas control valve for regulating a flow rate of the synthesis gas flowing into the heat exchanger; And a controller for controlling the heating amount of the heater, the opening amount of the syngas control valve, and the opening amount of the steam control valve.

A mixed gas thermometer for measuring the temperature of the mixed gas of the synthesis gas and steam introduced into the catalytic reactor; And a reactor thermometer for measuring a reaction temperature of the catalytic reactor, wherein the controller controls the heating amount of the heater, the opening amount of the syngas control valve, and the opening amount of the steam control valve, A syngas switching system for controlling the temperature can be provided.

A synthesis gas composition analyzer for analyzing a composition of the synthesis gas flowing into the heat exchanger; A syngas flow meter for measuring a flow rate of the synthesis gas flowing into the heat exchanger; A product gas composition analyzer for analyzing the composition of the product gas from which steam has been removed from the separator; And a product gas flow meter for measuring a flow rate of the product gas from which the steam has been removed in the separator, wherein the control unit controls the flow rate measured by the synthesis gas flow meter and the product gas flow meter, The CO conversion rate is calculated through the analyzer and the composition analyzed by the product gas composition analyzer and the calculated CO conversion rate is compared with the CO conversion rate required to modify the synthesis gas to a composition suitable for producing the raw material, And a syngas switching system for compensating the calculated difference value by adjusting the reaction temperature of the catalytic reactor.

A bypass line through which at least a portion of the syngas is provided to bypass the heat exchanger and the catalytic reactor; And a bypass valve controlling the flow rate of the bypass line and controlling the opening amount by the control unit.

A recovery line for cooling the generated gas in the cooler and recovering the discharged cooling water to the steam generator; And a return line for returning the liquefied steam to the steam generator in the separator.

Also, a syngas switching system may be provided wherein the mixed gas of the syngas and steam introduced into the catalytic reactor is dispersed in the internal space of the catalytic reactor through separate lines branched from the manifold.

Further, the reaction occurring in the catalytic reactor may be a conversion system of a syngas, which is a water gas conversion reaction.

According to another aspect of the present invention, there is provided a process for producing a syngas, comprising: supplying a synthesis gas containing CO and H ₂ synthesized with a syngas conversion system externally; Mixing the supplied syngas with steam; Reacting the mixed gas in which the synthesis gas and the steam are mixed in a catalytic reactor filled with a catalyst to reform it into a product gas; Exchanging the product gas and the syngas in a heat exchanger before the synthesis gas is mixed with steam; Cooling the product gas discharged after heat exchange; And liquefying and removing steam from the cooled product gas may be provided.

In addition, some of the syngas bypasses the catalytic reactor and the heat exchanger without mixing with the steam to generate a reformed gas by merging with the generated gas, and controls the flow rate of the bypassed synthesis gas, A method of converting a syngas to control the composition of the syngas can be provided.

The syngas heat-exchanged in the heat exchange step is heated by a heater, mixed with steam in the mixing step, and the heating amount of the heater, the flow rate of the synthesis gas, and the flow rate of steam are controlled, A method of converting a syngas to regulate the reaction temperature of the reactor can be provided.

Measuring a flow rate of the synthesis gas flowing into the heat exchanger; Analyzing the composition of the synthesis gas; Measuring a flow rate of the generated gas from which steam has been removed; And measuring the composition of the product gas from which steam has been removed, wherein the CO conversion rate is calculated through the measured flow rate of the synthesis gas and the product gas and the analyzed composition, and the synthesis gas is mixed with a composition suitable for producing a raw material There is provided a method of converting a syngas to compensate a calculated difference value by calculating a difference value by comparing the CO conversion target value required for reforming with the calculated CO conversion rate and adjusting the temperature to be reacted in the modifying step have.

According to the embodiments of the present invention, since the reaction heat of the catalytic reactor can be recycled and used to raise the temperature of the syngas, there is an effect that the thermal efficiency is increased.

Further, since the composition ratio of the synthesis gas can be controlled by controlling the reaction temperature of the catalytic reactor to control the conversion rate of the water gas conversion reaction, there is an effect that the control range of the composition ratio is wider than in the prior art.

1 is a conceptual diagram showing a conversion system of syngas according to an embodiment of the present invention.
Fig. 2 is a control block diagram of the syngas switching system of Fig. 1; Fig.
FIG. 3 is a graph showing the results of experiments on the conversion of CO conversion according to the reaction temperature of the water gas shift reaction in the catalytic reactor of FIG. 1.

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

In the following description of the present invention, detailed description of known functions and configurations incorporated herein will be omitted when it may make the subject matter of the present invention rather unclear.

FIG. 1 is a conceptual view showing a conversion system of a synthesis gas according to an embodiment of the present invention, and FIG. 2 is a control block diagram of a conversion system of the synthesis gas of FIG. 1.

1 and 2, a syngas conversion system 10 according to one embodiment of the present invention includes a catalytic reactor 100, a catalytic reactor 100, A cooler 300 for cooling the synthesis gas and the product gas discharged after heat exchange in the heat exchanger 200, and a process of the system And a control unit 400 for controlling the control unit 400.

In this embodiment, the synthesis gas is a gas produced by reacting carbon-based fuel with an oxidizing agent such as oxygen, steam or the like, and may be a gas mainly composed of CO and H ₂ . The synthesis gas can be supplied to the conversion process for obtaining raw materials used in the production of various fuels in a state where the composition ratio is appropriately controlled via the catalytic reactor 100.

The catalytic reactor 100 may be a reactor filled with a catalyst used for the catalytic reaction, and an Fe-based catalyst may be used as the catalyst to be filled. However, this is merely an example, and the catalyst used in the reaction may be any catalyst that can be used for the water gas conversion reaction. The catalytic reactor 100 may be configured to receive a mixed gas containing steam and a syngas to cause a reaction, and a catalyst packed therein may be used.

The mixed gas of the steam and the syngas supplied to the catalytic reactor 100 may be dispersedly supplied to each part of the catalytic reactor 100. To this end, the catalytic reactor 100 may be connected to a separate line 136 that branches off from the manifold 134 connected to the mixer 130. The mixed gas can be uniformly distributed over various portions of the internal space of the catalytic reactor 100 via the individual line 136 via the manifold 134. [ As a result, due to the water gas conversion reaction, which is an exothermic reaction, the temperature locally increases inside the catalytic reactor 100, and some of the internal catalysts become higher than the reaction limit temperature, Can be prevented.

The catalytic reactor 100 may be provided with a reactor thermometer 102 for measuring the reaction temperature and a process water supply unit 110, a steam generator 120, and a mixer 130 are provided at the front end of the catalytic reactor 100 .

The process water supply unit 110 may include a storage tank (not shown) for receiving and storing water from the outside and a pump and a valve (not shown) for supplying the stored water to the steam generator 120 as process water. have. The process water supplied from the process water supply unit 110 is supplied to the steam generator 120 so that steam can be produced.

The steam generator 120 is an apparatus for supplying steam to the process water to produce steam. The steam generator 120 may be an apparatus (for example, a heater) for converting energy from other types of energy (for example, electric energy) into heat energy And a heat exchanger for exchanging heat between the process water and the process water. A steam flow meter 122 for measuring the flow rate of steam and a steam control valve 124 for controlling the flow rate of steam may be disposed at a rear end of the steam generator 120. The steam flow meter 122 and the steam control valve 124 may be provided to the mixer 130 and mixed with the syngas.

The mixer 130 may be a device having a general configuration for mixing the two gases. The synthesis gas and the steam may be mixed and supplied to the mixer 130 and the mixed gas mixed in the mixer 130 may be supplied to the catalytic reactor 100 through the mixed gas thermometer 132 to perform a water gas conversion reaction have.

Meanwhile, the product gas discharged after the water gas conversion reaction in the catalytic reactor 100 is supplied to the heat exchanger 200, and heat exchange with the syngas can occur. For this purpose, a syngas supply unit 210 and a distributor 220 may be provided at the front end of the heat exchanger 200.

The syngas supply unit 210 can supply the synthesis gas generated by the reaction of the carbon-based fuel with the oxidant in the separately provided gasifier (not shown) and supply it to the distributor 220. To this end, the syngas supply unit 210 may include a gas storage tank (not shown) and a gas pump (not shown) and a valve (not shown) for storing syngas.

The syngas supplied from the syngas supply unit 210 may be supplied to the distributor 220 via a syngas composition analyzer 212 for analyzing the composition of the syngas. The distributor 220 may be a device for distributing the supplied synthesis gas to two lines, for example, a three-way valve. The distributor 220 may divide the synthesis gas into a line connected to the heat exchanger 200 and a bypass line 226 bypassing the heat exchanger 200.

The synthesis gas sent from the distributor 220 to the heat exchanger 200 can be supplied to the heat exchanger 200 via the synthesis gas flow meter 222 for measuring the flow rate and the synthesis gas control valve 224 for controlling the flow rate have. The syngas supplied to the heat exchanger 200 is heat-exchanged with the product gas discharged from the catalytic reactor 100 to increase the temperature. After heat exchange, the syngas is further heated by the heater 230 and supplied to the mixer 130 . The syngas supplied to the mixer 130 may be mixed with steam and supplied to the catalytic reactor 100 as described above.

The syngas bypassed through the bypass line 226 can be controlled in flow rate by the bypass valve 228 and merged with the synthesis gas discharged from the separator 320 to be described later to synthesize the raw material And can be provided as a conversion reactor for the < / RTI >

The generated gas discharged from the heat exchanger 200 after heat exchange may be transferred to the cooler 300 and cooled. The cooler 300 may be one of a heat exchanger for cooling generated gas to coolant, and may be connected to a coolant supply part 310 for supplying coolant. To this end, the cooling water supply unit 310 may include a cooling water storage tank (not shown) for receiving and storing cooling water from the outside, a pump (not shown) for transferring the cooling water, and a valve (not shown) for controlling the flow rate.

Cooling water having passed through the cooler 300 and having a high temperature after heat exchange with the generated gas is recovered through a recovery line 312 connected between the process water supply unit 110 and the steam generator 120, . ≪ / RTI > However, this is merely an example, and it is also possible that the coolant is discharged from the cooler 300 without being recovered.

The separator 320 may be provided at the rear end of the cooler 300 to separate and separate the steam contained in the generated gas. The steam liquefied by the separator 320 may be supplied to the recovery line 312 through the return line 322, And may be supplied to the steam generator 120.

The product gas from which the steam is separated through the separator 320 is passed through a bypass line 226 through a product gas composition analyzer 324 for analyzing the composition and a product gas flow meter 326 for measuring the flow rate, You can join. The gas in which the product gas and the synthesis gas passing through the bypass line 226 are mixed is a reformed gas because the synthesis gas is finally modified to have a desired composition. The reformed gas composition analyzer 328 may be provided at the rear end of the point where the synthesis gas passing through the bypass line 226 and the synthesis gas are merged to check whether the composition of the reformed gas is properly adjusted.

If the composition analysis shows that the composition of the reformed gas has been modified to a composition suitable for producing the raw material, the reformed gas can be transferred to the above-described conversion reactor.

The control unit 400 includes the steam flow meter 122, the synthesis gas composition analyzer 212, the synthesis gas flow meter 222, the product gas composition analyzer 324, the product gas flow meter 326, The syngas control valve 224, the bypass valve 228, and the heater 230, based on the values measured or analyzed from the thermometer 132 and the reactor thermometer 102. The operation of the steam control valve 124, As shown in FIG. For this, the control unit 400 may be a small built-in computer, for example, and may include a program, a memory, and a data processing unit including a CPU. The program includes a steam flow meter 122, a syngas composition analyzer 212, a syngas flow meter 222, a product gas composition analyzer 324, a product gas flow meter 326, a mixed gas thermometer 132, An algorithm for controlling the open amount of the steam control valve 124, the syngas control valve 224 and the bypass valve 228 and the calorific value of the heater 230 based on the values measured or analyzed from the reactor thermometer 102 . The program may be stored in a memory unit such as a computer storage medium, such as a flexible disk, a compact disk, a hard disk, or an MO (magneto optical disk), and installed in the control unit 400.

Hereinafter, the operation and effect of the syngas switching system 10 according to the present embodiment having the above-described structure will be described with reference to FIG. FIG. 3 is a graph showing the results of experiments on the conversion of CO conversion according to the reaction temperature of the water gas shift reaction in the catalytic reactor of FIG. 1.

Referring to FIG. 3, the syngas synthesized in the external gasifier may be supplied to the synthesis gas supply unit 210. The syngas supply unit 210 may supply the synthesis gas to the heat exchanger 200. At this time, the supplied synthesis gas may be analyzed through the synthesis gas composition analyzer 212 to analyze the composition of the synthesis gas, The composition ratio of CO and H ₂ contained in the synthesis gas can be analyzed in particular. The composition ratio of CO and H ₂ in the synthesis gas supplied by the synthesis gas supply unit 210 is generally about 1: 0.5 to 1, and the ratio of H ₂ is lower than that of CO. However, in order to produce the raw material using the synthesis gas, it is necessary to make the ratio of H2 higher than the ratio of CO, so it is necessary to modify the composition ratio of the synthesis gas through the water gas conversion reaction.

After the composition is analyzed by the synthesis gas composition analyzer 212, the synthesis gas is supplied to the distributor 220, and a part of the synthesis gas is supplied to the catalytic reactor 100 via the heat exchanger 200, And the remainder passes through the bypass line 226. At this time, the flow rate distributed to each line in the distributor 220 can be adjusted by controlling the opening amount of the control valves 224 and 228 disposed in each line. The measured value of the syngas flow meter 222 for measuring the flow rate of the synthesis gas supplied to the heat exchanger 200 may be fed back to the control unit 400 to be used for controlling the opening amount of the control valves 224 and 228 have.

The syngas introduced into the heat exchanger 200 receives heat from the product gas generated in the catalytic reactor 100 and is heated by the heater 230 after the heat exchange, To be mixed with the steam. At this time, the calorific value of the heater 230 can be controlled by the controller 400, and the calorific value of the heater 230 can be controlled by monitoring the temperature measured in the mixed gas thermometer 132 at the rear stage of the mixer 130 in real time .

Meanwhile, the process water supplied from the process water supply unit 110 is supplied to the cooling water from the cooler 300 through the recovery line 312, the liquefied steam delivered from the separator 320 through the return line 322, And may be introduced into the steam generator 120. The steam generator 120 may heat the inflowed water to change the steam into steam, and may transfer the steam to the mixer 130. At this time, the flow rate of the steam generated in the steam generator 120 can be measured by the steam flow meter 122, and the supply flow rate of the steam can be adjusted by the steam control valve 124. The flow rate of the steam measured by the steam flow meter 122 can be used to feedback control the opening amount of the steam control valve 124. The flow rate of the steam, which is changed according to the opening amount, is fed back to the controller 400, Amount can be controlled.

The mixed gas in which the steam and the syngas are mixed in the mixer 130 is transferred to the catalytic reactor 100 and may be contacted with the catalyst to cause a water gas conversion reaction. At this time, a plurality of individual lines 136 connected to the catalytic reactor 100 are dispersed from the manifold 134 connected to the mixer 130 such that the mixed gas is uniformly injected into each portion of the internal space of the catalytic reactor 100 Branch. Accordingly, the mixed gas can be uniformly dispersed and supplied into the catalytic reactor 100.

As a result, it is possible to prevent the local reaction from occurring inside the catalytic reactor 100, and the reaction can proceed throughout the interior space of the catalytic reactor 100.

The water gas conversion reaction occurring in the catalytic reactor 100 is an exothermic reaction in which carbon monoxide (CO) and steam (H ₂ O) contained in the syngas are reacted to generate carbon dioxide (CO ₂ ) and hydrogen (H ₂ ) Reaction. The conversion efficiency of the aqueous gas conversion reaction is determined according to the reaction temperature. When the Fe-based catalyst is used, the conversion efficiency can be determined by controlling the temperature within the range of 300 to 450 ° C. In other words, by controlling the reaction temperature in the catalytic reactor 100, the rate at which H ₂ is generated (CO conversion) as CO is converted to CO ₂ can be controlled.

Specifically, as can be seen from the graph of FIG. 3, the higher the reaction temperature in the reaction temperature range of 300 to 450 ° C., the higher the CO conversion rate. Since the reaction temperature can be indirectly controlled by controlling the temperature of the mixed gas introduced into the catalytic reactor 100, the CO conversion rate can also be controlled.

The reaction temperature of the catalytic reactor 100 may be measured by the reactor thermometer 102 and fed back to the controller 400 and the temperature of the mixed gas may be adjusted to match the feedback reaction temperature. The temperature of the mixed gas can be controlled by adjusting the calorific value of the heater 230, controlling the flow rate of the syngas, and controlling the flow rate of the steam. At this time, have.

Since the product gas generated through the reaction in the catalytic reactor 100 is a gas generated through an aqueous gas conversion reaction, which is an exothermic reaction, the temperature of the product gas is higher than that of the mixed gas introduced into the catalytic reactor 100, Can be introduced into the unit 200 and heat-exchanged with the syngas. As described above, since the synthesis gas is first heat-exchanged with the high-temperature production gas in the heat exchanger 200 before the synthesis gas is heated by the heater 230, the temperature of the synthesis gas can be increased, It saves the energy required to heat up as much as necessary. In other words, since the waste heat generated by the reaction occurring in the catalytic reactor 100 is recovered and used, the effect of improving the thermal efficiency can be achieved.

The generated gas, which has been desorbed from the syngas in the heat exchanger 200, is further transferred to the cooler 300 and can be cooled by the coolant. The generated gas delivered to the cooler 300 may be cooled to a temperature at which the steam contained in the product gas can be separated by the separator 320 at the subsequent stage and may be delivered to the separator 320.

The separator 320 may separate the steam contained in the generated product gas by liquefying it, and may include a cooling device (not shown) for this purpose. The product gas from which the steam is separated passes through the product gas composition analyzer 324, and the composition ratio is analyzed. The composition ratio can be analyzed after passing through the product gas flow meter 326. The values collected by the generated gas composition analyzer 324 and the generated gas flow meter 326 are transmitted to the controller 400. [

The control unit 400 may calculate the CO conversion rate based on the information collected from the synthesis gas composition analyzer 212, the synthesis gas flow meter 222, the product gas composition analyzer 324, and the product gas flow meter 326. Here, the CO conversion rate can be derived by the following equation.

The CO molar flow rate of the syngas in the above equation can be obtained through the composition ratio of CO analyzed by the synthesis gas composition analyzer 212 and the flow rate measured by the syngas flow meter 222, The composition ratio of CO analyzed in the analyzer 324 and the flow rate measured in the product gas flow meter 326.

Further, the control unit 400 can obtain the CO conversion target value required for modifying the composition of the synthesis gas supplied from the synthesis gas supply unit 210 to a composition suitable for the production of the raw material. The control unit 400 converts the calculated CO conversion rate into the CO conversion target value The difference value can be calculated. In order to compensate the calculated difference value, the CO conversion rate can be controlled by controlling the reaction temperature of the catalytic reactor 100 through controlling the calorific value of the heater 230, the flow rate of the syngas, and the flow rate of the steam.

On the other hand, the reformed gas when the composition analyzer 328, the higher the composition analysis result of the composition ratio of H ₂ in the desired H ₂ reformed gas than the composition ratio of the In, the synthesis gas flows together with the product gas through the bypass line 226, The H ₂ composition ratio of the reformed gas can be finally reduced by increasing the flow rate. Since the synthesis gas flowing through the bypass line 226 bypasses the catalytic reactor 100 and does not undergo a water gas conversion reaction, the composition ratio of H ₂ is small. Therefore, when the flow rate of the synthesis gas flowing through the bypass line 226 is increased, the synthesis gas is mixed with the product gas, resulting in lowering the H ₂ composition ratio of the reformed gas.

Through this process, it is possible to modify the synthesis gas to a desired composition, and the modified synthesis gas can be transferred to the conversion reactor at the downstream stage of the system and converted into the raw material.

According to the above-described synthesis gas switching system 10, since the reaction heat of the catalytic reactor 100 can be used to increase the temperature of the synthesis gas required for the reaction, the thermal efficiency of the entire system is increased . Further, since the composition ratio of the synthesis gas can be controlled by controlling the reaction temperature of the catalytic reactor 100 and controlling the CO conversion of the water gas conversion reaction, the control range of the composition ratio is wider than in the past, and stable and efficient composition ratio control is possible .

While the present invention has been described in connection with certain exemplary embodiments thereof, it is to be understood that the invention is not limited to the specific embodiments thereof except as defined in the appended claims. . Skilled artisans may implement a pattern of features that are not described in a combinatorial and / or permutational manner with the disclosed embodiments, but this is not to depart from the scope of the present invention. It will be apparent to those skilled in the art that various changes and modifications may be readily made without departing from the spirit and scope of the invention as defined by the appended claims.

10: Synthetic gas conversion system 100: Catalytic reactor
102: Reactor thermometer 110: Process water supply unit
120: Steam generator 122: Steam flow meter
124: Steam control valve 130: Mixer
132: mixed gas thermometer 134: manifold
136: individual line 200: heat exchanger
210: Synthetic gas supply unit 212: Synthetic gas composition analyzer
220: Dispenser 222: Syngas flow meter
224: Synthetic gas control valve 226: Bypass line
228: Bypass valve 230: Heater
300: cooler 310: cooling water supply part
312: recovery line 320: separator
322: Return line 324: Produced gas composition analyzer
326: Generated gas flow meter 328: Reformed gas composition analyzer
400:

Claims (11)

A catalytic reactor for reacting a synthesis gas containing CO and H ₂ with steam generated by a steam generator to change a composition ratio of CO and H ₂ of the synthesis gas;
A steam control valve for controlling a flow rate of steam flowing into the catalytic reactor;
A heat exchanger for heat-exchanging the syngas produced by the reaction in the catalytic reactor;
A heater for heating the syngas discharged from the heat exchanger after heat exchange with the product gas;
A cooler for cooling the produced gas discharged from the heat exchanger after heat exchange with the syngas;
A separator for liquefying and separating steam contained in the product gas cooled in the cooler;
A syngas control valve for regulating a flow rate of the synthesis gas flowing into the heat exchanger;
A control unit for controlling a heating amount of the heater, an opening amount of the syngas control valve, and an opening amount of the steam control valve;
A mixed gas thermometer for measuring the temperature of the mixed gas of the synthesis gas and the steam introduced into the catalytic reactor;
A reactor thermometer for measuring a reaction temperature of the catalytic reactor;
A synthesis gas composition analyzer for analyzing a composition of the synthesis gas flowing into the heat exchanger;
A syngas flow meter for measuring a flow rate of the synthesis gas flowing into the heat exchanger;
A product gas composition analyzer for analyzing the composition of the product gas from which steam has been removed from the separator; And
And a product gas flow meter for measuring the flow rate of the product gas from which steam has been removed in the separator,
Wherein,
Controlling a reaction temperature of the catalytic reactor by controlling a heating amount of the heater, an opening amount of the syngas control valve, and an opening amount of the steam control valve,
The CO conversion rate is calculated through the flow rate measured by the syngas flow meter and the product gas flow meter and the composition analyzed by the synthesis gas composition analyzer and the product gas composition analyzer,
Calculating a difference value by comparing the CO conversion target value required for modifying the synthesis gas to a composition suitable for producing the raw material and the calculated CO conversion rate,
And the difference value is calculated by adjusting the reaction temperature of the catalytic reactor. delete delete The method according to claim 1,
A bypass line through which at least a portion of the synthesis gas is provided to bypass the heat exchanger and the catalytic reactor; And
Further comprising a bypass valve for controlling a flow rate of the bypass line and controlling an opening amount by the control unit. The method according to claim 1,
A recovery line for cooling the generated gas in the cooler and recovering the discharged cooling water to the steam generator; And
And a return line for returning the liquefied steam to the steam generator in the separator. The method according to claim 1,
Wherein the mixed gas of the synthesis gas and the steam introduced into the catalytic reactor is dispersed and supplied to the inner space of the catalytic reactor through separate lines branched from the manifold. 7. The method according to any one of claims 1 and 4 to 6,
Wherein the reaction occurring in the catalytic reactor is a water gas conversion reaction. A synthesis gas containing CO and H ₂ synthesized by a conversion system of synthesis gas from outside is supplied;
Mixing the supplied syngas with steam;
Reacting the mixed gas in which the synthesis gas and the steam are mixed in a catalytic reactor filled with a catalyst to reform it into a product gas;
Exchanging the product gas and the syngas in a heat exchanger before the synthesis gas is mixed with steam;
Cooling the product gas discharged after heat exchange;
Liquefying and removing steam from the cooled product gas;
Measuring a flow rate of the synthesis gas flowing into the heat exchanger;
Analyzing the composition of the synthesis gas;
Measuring a flow rate of the generated gas from which steam has been removed; And
Measuring the composition of the product gas from which steam has been removed,
Exchanging the heat-exchanged synthesis gas with the heater in the heat exchange step, mixing the steam with the steam in the mixing step,
Controlling a reaction temperature of the catalytic reactor by controlling a heating value of the heater, a flow rate of the syngas, and a flow rate of steam,
A CO conversion rate is calculated through the measured flow rate of the synthesis gas and the generation gas and the analyzed composition,
Calculating a difference value by comparing the CO conversion target value required for modifying the synthesis gas to a composition suitable for producing the raw material and the calculated CO conversion rate,
And adjusting the temperature at which the reaction is performed in the reforming step to compensate the calculated difference value. 9. The method of claim 8,
A part of the syngas bypasses the catalytic reactor and the heat exchanger without mixing with the steam to join with the product gas to generate a reformed gas,
And controlling the flow rate of the bypassing syngas to control the composition of the reformed gas. delete delete

Images