Reforming method of reducing gas for syngas production and reforming process system therefor

Abstract

The present invention relates to a reforming method of reducing gas for syngas production and a reforming process system therefor and, more specifically, to a reforming method suitable for continuously producing syngas through the reforming reaction of reducing gas by continuously using an oxidizing agent without interruption of the process, utilizing a catalyst for reforming reactions, and a reforming process system using same.

Description

Reforming method of reducing gas for synthesis gas production and its reforming process system

[0001] The present invention relates to a method for reforming a reducing gas for producing synthesis gas and a reforming process system thereof, and more particularly, to a suitable reforming method for producing synthesis gas through a reforming reaction of a reducing gas using a catalyst for reforming reaction and an oxidizing agent continuously without interruption of the process, and a reforming process system using the same.

[0002] Unless otherwise indicated herein, the materials described in this section are not prior art to the claims of this application, and their inclusion in this section is not intended to be admitted as prior art.

[0003] Recently, energy issues have become a major social issue, and on the other hand, excessive greenhouse gas emissions related to carbon dioxide emissions are emerging as a serious environmental problem.

[0004] Recognizing the urgent need to develop and utilize renewable energy sources that can achieve sustainable growth to secure energy security both domestically and internationally, renewable energy sources are being expanded, and various technologies are being developed to address environmental issues, such as carbon dioxide capture and utilization.

[0005] Our country is recognized as a major greenhouse gas emitter in the world, and international pressure to reduce greenhouse gas emissions is increasing.

[0006] Hydrogen energy is being utilized as a future clean energy source that can simultaneously solve environmental problems such as global warming and the problem of energy dependence, and securing technology to utilize carbon dioxide as a cyclical carbon resource is becoming an important research topic.

[0007] In general, there are methods for producing synthesis gas composed of hydrogen and carbon monoxide, including methods using fossil fuels such as natural gas. Among these synthesis gas production methods, from an economic perspective, it is advantageous to use biomass such as carbon dioxide and methane gas and utilize renewable energy.

[0008] As a method for producing synthesis gas from such biogas, methods known include dry reforming, wet reforming, and combined reforming, which are summarized in the following reaction formula, depending on the input conditions of carbon dioxide, water, etc. in the reforming reaction of reducing gas.

[0009] Dry reforming: CO2+ CH4→ 2CO + 2H2O (ΔH=261 kJ / mol)

[0010] Wet reforming: H2O + CH4→ 3H2+ CO (ΔH=226 kJ / mol)

[0011] Complex reforming: CO2+ 3CH4+ 2H2O → 4CO + 8H2 (ΔH=712 kJ / mol)

[0012] Among the reforming reactions using the above-mentioned reducing gas, dry reforming is a synthesis gas production technology that can use the largest amount of CO2 (greenhouse gas) as a raw material among catalytic reforming technologies, and is attracting worldwide interest in securing the technology due to its high greenhouse gas reduction effect.

[0013] In particular, the dry reforming reaction requires a higher proportion of CO2 for chemical product production than other reforming reactions and has a high impact on greenhouse gas reduction, so efforts are being made to secure excellent reaction technology.

[0014] However, in this dry reforming reaction, a catalyst is used to carry out the reaction, and the dry reforming (DRM) technology that can reduce greenhouse gases has a fatal drawback that makes commercialization difficult due to the short lifespan of the catalyst.

[0015] In this way, existing dry reforming catalysts have been continuously developed for the past 100 years because they can use CO2 as a raw material, but they still have the problem of extremely limited lifespan due to deactivation of the catalyst surface.

[0016] Therefore, while various studies have been proposed to extend the life of catalysts in dry reforming, technical approaches other than those that utilize specific catalyst compositions to extend life are lacking. Consequently, process proposals for this dry reforming method are practically challenging.

[0017] As a conventional dry reforming reaction process, a method for producing hydrogen including a reactive regeneration process including a methane-carbon dioxide dry reforming reaction is proposed in Korean Patent Publication No. 10-2022-0129702.

[0018] In addition, various methods for producing synthesis gas by dry reforming using dry reforming catalysts or wet or complex reforming reactions have been proposed, but most of them only propose methods that depend on the catalyst composition and do not provide improvements for a series of continuous reaction processes.

[0019] Therefore, there is an urgent need to develop a reforming method and system suitable for application to the reforming reaction process that produces synthesis gas using reducing gases such as methane, and in particular, a method for producing synthesis gas, etc., by using a catalyst for a long period of time without carbon deposition.

[0020] {Prior art literature}

[0021] [Patent Document]

[0022] (Patent Document 1) Korean Patent Publication No. 10-2022-0129702

[0023] The present invention aims to solve the problems of the prior art as described above by developing a method for reforming a reducing gas and a system thereof, which are suitable for performing a reforming reaction of a reducing gas effectively using a reforming reaction catalyst to produce a synthesis gas, and in particular, for performing the reforming process continuously without process interruption.

[0024] Accordingly, the purpose of the present invention is to provide a method for reforming a reducing gas, which produces a synthesis gas by reforming the reducing gas using an oxidizing agent and a catalyst for reforming reaction.

[0025] In addition, another object of the present invention is to provide a reforming method for effectively producing synthesis gas by enabling continuous reforming reaction without interruption of the process in the reforming reaction of reducing gas.

[0026] In addition, another object of the present invention is to provide a reforming process system for reducing gas that can produce synthesis gas by replacing a catalyst or removing carbon without stopping the process by using a catalyst for reforming reaction.

[0027] The purpose of the present invention is not limited to the above-mentioned purpose, and should be understood to include all purposes that can be inferred from the composition of the invention described in the detailed description or claims of the present invention, or all purposes that can be achieved by the description or technical idea of ​​the present invention.

[0028] In order to solve the above-described problem of the present invention, the present invention provides a method for reforming a reducing gas for producing a synthesis gas, comprising the steps of: injecting an oxidizing agent and a reducing gas raw material; performing a reforming reaction using a catalyst for reforming; cooling the synthesis gas obtained by the reforming reaction and recovering waste heat; drying and separating water; separating a product gas; and returning unreacted matter from the separation step back to the raw material injection step and mixing it with the injected raw material.

[0029] According to a preferred embodiment of the present invention, the raw material can be injected with a reducing gas and an oxidizing agent in a volume ratio of 1:0.5 to 10.

[0030] According to a preferred embodiment of the present invention, in the step of performing a reforming reaction, it is preferable to include a step of arranging the catalyst for the reforming reaction in a plurality of reaction lines so as to have multiple flow paths within the reactor and causing the reaction.

[0031] According to a preferred embodiment of the present invention, in the step of performing the above modification reaction, the reaction temperature may be set to 700 to 1200°C.

[0032] According to a preferred embodiment of the present invention, a carbon removal step may be included after the reforming reaction.

[0033] According to a preferred embodiment of the present invention, the carbon removal step may include a step of removing carbon by adding an oxidizing agent or physically removing carbon.

[0034] According to a preferred embodiment of the present invention, the step of removing carbon using the oxidizing agent may include a method of removing carbon by converting it into CO or CO2 by supplying one or more oxidizing agents among Air, O2, H2O, and CO2 to the syngas generated after the reforming reaction at 400 to 800°C.

[0035] According to a preferred embodiment of the present invention, the step of physically removing carbon may include a method of configuring two or more flow lines of syngas generated after a reforming reaction in parallel so that carbon accumulated in one of the flow lines is physically removed while transferring the syngas to another flow line.

[0036] According to a preferred embodiment of the present invention, the synthesis gas may be separated into CO and H2 using at least one of PSA, membrane, and cold box.

[0037] According to a preferred embodiment of the present invention, the metal oxide may be any catalyst useful for a reforming reaction by dry reforming, wet reforming or composite reforming, and may contain, for example, at least one selected from oxides of nickel, cobalt, iron, copper, vanadium, molybdenum, platinum metals, cerium, ruthenium, rhodium, palladium or zirconium.

[0038] The present invention provides a reforming process system for producing synthesis gas, which can apply the above-described method for reforming a reducing gas, comprising: a raw material injection unit for injecting an oxidizing agent and a reducing gas raw material; a reforming reactor including a catalyst for reforming reaction and performing a reforming reaction of the reducing gas raw material; a cooler for cooling the synthesis gas obtained by the reforming reaction and recovering waste heat; a dryer for drying the synthesis gas and separating water; a product separation and purification unit for separating the synthesis gas; and a circulation line for returning unreacted materials from the separation step back to the raw material injection step and mixing them with the injected raw material.

[0039] According to a preferred embodiment of the present invention, an oxidizing agent addition reaction means or a physical removal means may be included between the reforming reactor and the cooler as a means for removing carbon.

[0040] As described above, the method for reforming a reducing gas according to the present invention has an effect of being economically applicable to a reforming reaction process of a reducing gas by applying a reforming reaction process that can be used for a long period of time without carbon deposition with a process configuration that has not been previously proposed.

[0041] In particular, since the reforming reaction process of the present invention can continuously perform the reforming reaction using a catalyst without stopping the process, it has the effect of being able to perform a large-scale reaction process that can utilize carbon, such as producing hydrogen using carbon-based greenhouse gases such as carbon dioxide and methane, in an automated manner.

[0042] Therefore, the present invention has great practical value in that it provides a method for reforming a reducing gas and a reforming process system as an environmentally friendly manufacturing process that reduces greenhouse gases and achieves carbon neutrality.

[0043] Figure 1 is a drawing that briefly shows a process diagram to which a modification method according to the present invention is applied.

[0044] Figure 2 is a conceptual diagram showing a state of multiple catalyst arrangements, exemplifying a state in which catalysts for reforming reactions are arranged in parallel in three reaction lines in a reforming process system according to the present invention.

[0045] Figure 3 is a partial process diagram illustrating a process of removing carbon using an oxidizer by configuring a flow line of synthesis gas in parallel according to the present invention.

[0046] Figure 4 is a partial process diagram illustrating a process for physically removing carbon by configuring a flow line of synthesis gas in parallel according to the present invention.

[0047] Figure 5 is a graph comparing the results of the conversion rate for the composition of each component in the reaction temperature range according to the reforming reaction in an experimental example of the present invention and the change in the amount of each component used according to the reaction temperature.

[0048] Hereinafter, the present invention will be described in more detail as an embodiment.

[0049] The present invention relates to a reforming method for reforming a reducing gas using a catalyst for reforming reaction, as illustrated in the process diagram of FIG. 1.

[0050] The reducing gas used as a raw material in the present invention is defined as a reducing agent for components used in a carbon reaction system, such as producing synthesis gas by reducing CO2, and mostly refers to a gaseous substance. Such reducing gases include hydrocarbons such as methane, ethane, and propane, or mixtures thereof, or compounds in which these are mixed. Examples of reducing gases may include mixtures of CH4, CO2, H2, O2, and N2.

[0051] Additionally, reducing gases typically include biogas, industrial by-product gases from industrial activities, mixed gases, greenhouse gases such as methane, unreacted products, by-products, and volatile organic compounds generated in factories. Examples of biogas include methane, ethane, propane, butane, alcohols, ketones, and aldehydes.

[0052] In the present invention, the oxidizing agent refers to an agent that can react with the reducing gas to cause a reforming reaction. For example, one or more of Air, O2, H2O, and CO2 may be used. Most preferably, one or more of H2O and CO2 may be used. The oxidizing agent in the present invention includes a reaction in which carbon deposition occurs during the reforming reaction process involving the above-mentioned reducing gas.

[0053] In the present invention, as raw materials for the reforming reaction, oxidizing agents and reducing gases may be used, and in particular, for typical dry reforming or complex reforming reactions, for example, carbon dioxide and methane, or carbon dioxide, water, and methane may be used.

[0054] According to a preferred embodiment of the present invention, these raw materials can be injected into the reaction process at a predetermined ratio for the reforming reaction.

[0055] According to a preferred embodiment of the present invention, when the reducing gas and oxidizing agent injected as raw materials are injected in a volume ratio of 1:0.5 to 10, excellent results can be obtained in the conversion rate of the reducing gas. If the content ratio is outside the above range, the conversion rate may be significantly reduced, and if the oxidizing agent is less than the reducing gas, for example, the amount of carbon generated may increase rapidly, and if it is too excessive, the economic efficiency in the separation and purification section may decrease, and as the flow rate increases, there is a problem in that the product production amount may decrease.

[0056] According to the present invention, after the raw material is injected, the reducing gas as described above undergoes a reforming reaction.

[0057] According to a preferred embodiment of the present invention, in the step of performing the above-described reforming reaction, the reaction temperature may be set to 700 to 1,200°C, more preferably 800 to 1,000°C.

[0058] According to a preferred embodiment of the present invention, this reforming reaction is carried out under a reforming reaction catalyst, and it is preferable to use a catalyst for this reforming reaction that does not cause carbon deposition.

[0059] According to a preferred embodiment of the present invention, it is preferable that the catalyst for the reforming reaction is arranged in a plurality of reaction lines so as to have multiple flow paths within the reactor during the step of performing the reforming reaction, thereby including a step of reacting the catalyst.

[0060] Such a catalyst arrangement method is such that, when using three arrangement structures of catalysts, as exemplified in Fig. 2, for example, the reaction occurs in the first arrangement, and the second arrangement can be replaced when the first arrangement is used for a long period of time or when the reaction conditions deteriorate, so that the second arrangement can be used as a replacement to enable continuous reforming reaction by moving the reforming reaction line. In addition, the third arrangement can be used as a method of additionally preparing it as a spare.

[0061] According to the present invention, in some cases, the plurality of catalyst reaction lines may be arranged in two or four or more, and in the case where three or more are arranged as in FIG. 2, the reaction may be performed in two or more of the plurality of lines, and the remaining arrangement lines may be used for replacement, reserve, etc.

[0062] According to a preferred method of the present invention, after the reforming reaction using the catalyst is completed as described above, a step is performed to cool the synthesis gas obtained through the reforming reaction and recover waste heat. This waste heat recovery is significant in that it can be utilized as an energy source.

[0063] According to the present invention, after recovering waste heat from the product after the reforming reaction as described above, a drying process is performed to separate water generated as a reaction product.

[0064] On the other hand, a product separation step is performed to separate the synthesis gas generated by the above reforming reaction. In this separation step, unreacted materials are returned to the raw material injection step and circulated through a circulation line, thereby undergoing a step of mixing with the injected raw material.

[0065] According to a preferred embodiment of the present invention, the generated synthesis gas may include separating CO and H2 at high purity using at least one of PSA, membrane, and cold box.

[0066] Meanwhile, in the reforming reaction process of the present invention, a reforming catalyst is used. According to a preferred embodiment of the present invention, the reforming reaction catalyst may be a catalyst in which a metal oxide catalyst is dispersed on a support.

[0067] According to the present invention, the metal oxide may contain at least one selected from oxides of nickel, cobalt, iron, copper, vanadium, molybdenum, platinum metals, cerium, ruthenium, rhodium, palladium, or zirconium.

[0068] In particular, the present invention confirmed that, in the case of reforming catalysts, the cause of catalyst surface deactivation and formulation damage is carbon deposition (coking). Therefore, the present invention applies a method for removing such carbon deposition, enabling continuous reforming reactions without process interruption for catalyst replacement or other reasons.

[0069] The present invention includes a reducing gas reforming process system that can utilize the above-described reducing gas reforming method.

[0070] A preferred reforming process system according to the present invention may have a configuration as illustrated in FIG. 1, for example. In FIG. 1, for the purpose of facilitating understanding, an example is provided in which carbon dioxide is used as an oxidizing agent and methane is used as a reducing gas.

[0071] The system of the present invention can be configured to include, for example, a raw material injection unit (11) for injecting an oxidizing agent and a reducing gas raw material; a reforming reactor (12) including a catalyst for reforming reaction and performing a reforming reaction of the raw material; a cooler (13) for cooling a synthesis gas (12a) obtained by the reforming reaction and recovering waste heat; a dryer (14) for drying the synthesis gas and separating water; a product separation and purification unit (15) for separating the generated gas; and a return line (16) for returning unreacted materials from the separation step back to the raw material injection step and mixing them with the injected raw material.

[0072] According to a preferred embodiment of the present invention, the catalyst used in the reforming reactor (12) may comprise a structure arranged in multiple lines, for example. A typical example of such a configuration is illustrated in FIG. 2. Here, the reforming reaction of carbon dioxide and methane is illustrated as an example. When the catalyst is arranged in multiple reaction lines, each catalyst arrangement line can be used for reaction, replacement, or reserve purposes during the reforming reaction process.

[0073] According to a preferred embodiment of the present invention, a sensor for checking the injection amount of the reaction raw material injected into the reactor (12) and a detection sensor for detecting in advance the time for replacement of the reforming catalyst may be included.

[0074] Additionally, according to a preferred embodiment of the present invention, a carbon removal step may be included after the reforming reaction. Since carbon may be generated as a result of a side reaction during the reforming reaction, this carbon must be removed to ensure stable operation without blockage in the product transport line.

[0075]

[0076] *Therefore, according to the drawing 2 of the present invention, the reforming catalyst installation part (121) corresponding to the part where carbon, which is bound to be generated at a specific temperature due to a side reaction, accumulates is installed in parallel, and when a certain amount of carbon accumulates therein, the part is excluded and the product flows to another part, and the part previously used can be applied with a system that removes carbon by adding an oxidizer to remove the carbon, for example. The oxidizer that can be used here can be Air, O2, H2O, CO2, and the supply line can be configured to pass inside a heating means such as a burner so as to be preheated to a temperature higher than that required for carbon removal.

[0077] According to a preferred embodiment of the present invention, the carbon removal step may include a step of removing carbon by adding an oxidizing agent (122) as illustrated in FIG. 3, for example, or a step of physically removing carbon as illustrated in FIG. 4. Here, a reforming reaction of carbon dioxide and methane is illustrated as an example.

[0078] According to a preferred embodiment of the present invention, the step of removing carbon using the oxidizing agent may include a method of supplying one or more oxidizing agents among Air, O2, H2O, and CO2 to the syngas generated after the reforming reaction at 400 to 800°C to convert and remove carbon into CO or CO2. More preferably, it is good to supply the oxidizing agent at 500 to 600°C to remove carbon. If the temperature is too low, the oxidation reaction by the oxidizing agent does not occur properly, making carbon removal difficult, and if the temperature is too high, the reaction heat generated during the oxidation process may be added, which may put a strain on the equipment. In addition, it is preferable to use Air as the oxidizing agent here in terms of stability.

[0079] According to a preferred embodiment of the present invention, in order to remove carbon deposited on a catalyst in the above-described reforming process, for example, an oxidizing agent addition reaction means for carbon removal between a reforming reactor and a cooler may include a carbon removal means that forms a plurality of product transfer lines having valves so that while carbon is removed by supplying an oxidizing agent in one transfer line (VALVE1), a product is supplied through another transfer line (VALVE2), and such a process is alternately and repeatedly performed.

[0080] For this purpose, a process such as that illustrated in Fig. 3 may be employed. Fig. 3 is a partial process diagram illustrating a process of removing carbon using an oxidizer by configuring a synthesis gas flow line in parallel according to the present invention. As an example, the reforming reaction of carbon dioxide and methane is illustrated here.

[0081] Referring to Fig. 3, an example is provided. After reforming, the product passes through the dry reforming reactor and moves to the cooler via VALVE1. During this process, if carbon accumulates in the downstream equipment of VALVE1, such as between the reforming reactor and the cooler or in the cooler, it becomes difficult to continuously perform the process. Therefore, VALVE1 can be locked and the product can be transferred via VALVE2. This way, the product transfer line is controlled so that it is transferred via the transfer line of VALVE2.

[0082] At this time, VALVE1-1 is opened to supply OA (oxidizer, 122) to the downstream equipment of the VALVE1 line where carbon is deposited. In order to raise the temperature required to remove carbon deposited in the downstream equipment while supplying the oxidizer in this way, the supplied oxidizer can be designed to increase its temperature as it passes through the inside of the burner.

[0083] Through this process, when the carbon deposited in the downstream equipment of the transfer line of VALVE1 is removed, VALVE1 and VALVE1-1 are kept locked and waited until carbon is deposited again in the downstream equipment of the transfer line of VALVE2, which is the opposite transfer line.

[0084] According to a preferred method of the present invention, in the reforming process, the product is transported using VALVE2 as a transport line during carbon removal in the VALVE1 transport line, and conversely, the process can be carried out using a system that uses VALVE1 as a transport line during carbon removal in the VALVE2 transport line.

[0085] In this way, according to a preferred embodiment of the present invention, continuous operation can be performed without interruption in the transport of the product by alternately using the transport line of VALVE1 and the transport line of VALVE2 to remove carbon on one side while transporting the product on the other side.

[0086] Figure 4 illustrates a case where a physical method is used for carbon removal. As an example, the reforming reaction of carbon dioxide and methane is illustrated.

[0087] According to a preferred embodiment of the present invention, when using a step of physically removing carbon as shown in FIG. 4, a method may be included in which the flow lines (123) of the synthesis gas (12a) generated after the reforming reaction are configured in two to three, preferably two, parallel lines, so that carbon accumulated in one flow line is physically removed while the synthesis gas is transferred to the other flow line. If configured with three flow lines, one flow line can be used as a reserve, or two flow lines (123) can be used, and carbon can be physically removed from the flow line in which carbon deposition occurs first, and the flow of the synthesis gas can be maintained in the other flow line.

[0088] According to a preferred embodiment of the present invention, the physical carbon removal method used herein may be performed by, for example, a method of directly scraping using a brush or a method of orthogonally replacing in the form of a cartridge.

[0089] Thus, when performing a reforming reaction on a reducing gas using the reforming method and reforming process system according to the present invention, even if carbon deposition occurs, continuous carbon removal is possible without interruption of the process. Furthermore, more preferably, dry reforming can be performed continuously without interruption of the process, even during the carbon removal or replacement process.

[0090] Therefore, it is very useful for reforming raw materials of oxidizing agents and reducing gases, and it is possible to perform continuous mass reaction processes in an automated manner while being economical.

[0091] Therefore, according to a preferred embodiment of the present invention, a preferable example of applying the method and reforming process system of the reducing gas of the present invention is that when methane, which is a reducing gas, is reformed using carbon dioxide as an oxidizing agent, a very effective dry reforming or combined reforming medium is applied, thereby realizing carbon neutrality and utilizing greenhouse gases, and it can be utilized as a very useful process in that it can be performed as a large-scale automated continuous process.

[0092]

[0093] Hereinafter, the present invention will be described in detail based on examples, but the present invention is not limited to the examples.

[0094] <Example>

[0095] A dry reforming reaction was performed using carbon dioxide and methane gas as raw materials in the composition ratios shown in Table 1 below. A nickel-cobalt catalyst (nickel:cobalt = 1:5) was used as the catalyst for the reaction.

[0096] The dry reforming reaction was performed using a process line prepared with the process equipment of Fig. 1, and the reforming reaction was performed according to the following reaction formula.

[0097] [Reaction formula]

[0098] CH4decomposition: CH4↔ C(s) + 2H2

[0099] CO disassociation: 2CO ↔ C(s) + CO2

[0100] CO2gasification: C + CO2↔ 2CO

[0101] According to the process diagram of Fig. 1, the reaction was carried out in the following steps.

[0102] a) CO2: CO2 supply line (11)

[0103] b) CH4: LNG supply line (11)

[0104] c) MIXER: The part where unreacted substances are mixed after separation from CO2, CH4, and SEPMD.

[0105] d) REACTANT: Transfer line for injection from MIXER to reactor

[0106]

[0107] * e) REACTOR: Reforming reactor (12)

[0108] f) SYNGAS: A line through which the synthesis gas (12a) generated in the reforming reactor is transferred to a cooler (13) and a dryer (14), which are heat exchangers.

[0109] g) COOLER: A cooler (13) that cools high-temperature synthesis gas and recovers waste heat.

[0110] h) DRYER: Dryer as a water removal device for SEPMD (14)

[0111] i) H2O: Line that transports water removed from the DRYER

[0112] j) SEPMD: A separator (15) as a device that separates CO and H2 of desired purity by selecting the separation method of PSA as a synthesis gas separation module.

[0113] k) CO: A line that transports high-purity CO separated from SEPMD.

[0114] l) H2: A line that transports high-purity H2 separated from SEPMD.

[0115] m) RECYCLE: A circulation line (16) that transfers unreacted material separated from SEPMD to a reforming reactor.

[0116] n) DETEC1: A device that analyzes the composition of reactants in real time.

[0117] o) DETEC2: A device that analyzes the composition of products from which water has been removed in real time.

[0118] p) CW1, CW2: Lines transporting cooling water

[0119] In the above process, in order to supply reactants and collect products suitable for a continuous process, the supply of CO2 is adjusted based on the real-time analysis results of DETEC1, and the ratio of products and reactants of CO2 and CH4 that can prevent carbon deposition are adjusted to ensure a stable continuous process.

[0120] In addition, a sensor that can detect the timing of catalyst replacement in advance is attached, and based on the real-time analysis results of DETEC2, when the CH4 concentration reaches 80% of the maximum CH4 concentration required by SEPMD, the flow of CO2 and CH4 is reduced to maintain operation, and when the production volume falls below the desired level, the catalyst is replaced.

[0121] The reaction temperature of the above reforming reactor was maintained at 800 to 1000°C, and after the reaction, the reactants CO and H2 were separated with high purity.

[0122]

[0123] <Experimental Example>

[0124] The composition of the reaction product obtained at the reactor outlet according to the raw material ratio for the reforming reaction performed using the above method and system is shown in Table 1 below.

[0125]

[0126] Referring to the results of the composition of each component in the reaction temperature range according to the above dry reforming reaction, the change in the amount of each component used according to the reaction temperature is shown in the graph of Fig. 5.

[0127] [Explanation of symbols]

[0128] 11 - Raw material injection line

[0129] 12 - Reforming reactor

[0130] 12a - Syngas

[0131] 13 - Cooler

[0132] 14 - Dryer

[0133] 15 - Separator

[0134] 16 - Circular line

[0135] 121 - Reforming catalyst installation section

[0136] 122 - Oxidizer

[0137] 123 - Flow Line

Claims

1. A step of injecting an oxidizing agent and a reducing gas raw material; a step of performing a reforming reaction using a catalyst for a reforming reaction; A step of cooling the synthesis gas obtained through the reforming reaction and recovering waste heat; Drying and water separation step; A product separation step for separating synthesis gas; and In the separation step, unreacted materials are circulated back to the raw material injection step and mixed with the injected raw materials. A method for reforming reducing gas for producing synthesis gas including .

2. A method for reforming a reducing gas, characterized in that in claim 1, methane gas and carbon dioxide are injected as raw materials in a volume ratio of 1:0.5 to 10 as a reducing gas and an oxidizing agent.

3. A method for reforming a reducing gas, characterized in that in claim 1, in the step of performing a reforming reaction, a catalyst for the reforming reaction is arranged in a plurality of reaction lines so as to have multiple flow paths within the reactor and reacted.

4. A method for reforming a reducing gas, characterized in that in the step of performing the reforming reaction in claim 1, the reaction temperature is 700 to 1,200°C.

5. A method for reforming a reducing gas, characterized in that it includes a method of removing carbon by converting it into CO or CO2 by supplying at least one oxidizing agent among Air, O2, H2O, and CO2 to the syngas produced after the reforming reaction at 400 to 800°C in claim 1.

6. A method for reforming a reducing gas, characterized in that it comprises a method of configuring two or more flow lines of a synthesis gas (syngas) produced after a reforming reaction in parallel in claim 1, so that carbon is accumulated in one of the flow lines and physically removed while transferring the synthesis gas to another flow line.

7. A method for reforming a reducing gas, characterized in that in claim 1, the synthesis gas is separated using at least one of PSA, membrane, and cold box.

8. A reforming process system for reforming reaction of reducing gas, comprising: a raw material injection unit for injecting an oxidizing agent and reducing gas raw material; A reforming reactor that includes a catalyst for reforming reaction and performs reforming reaction of a reducing gas raw material by utilizing an oxidizing agent; A cooler that cools the synthesis gas obtained through the reforming reaction and recovers waste heat; A dryer that dries the synthesis gas and separates the water; A product separation and purification unit for separating synthesis gas; and A circulation line that returns unreacted materials from the separation stage back to the raw material injection stage and mixes them with the injected raw materials. A reforming process system for reducing gas for producing synthesis gas including .

9. A reducing gas reforming process system according to claim 8, characterized in that it includes an oxidizing agent addition reaction means or a physical removal means as a means for removing carbon between the reforming reactor and the cooler.

10. A reducing gas reforming process system according to claim 9, characterized in that the oxidizing agent addition reaction means forms a plurality of product transfer lines having valves, and includes a carbon removal means for supplying products through transfer lines of other parts while removing carbon through oxidizing agent supply in some transfer lines, and for performing these processes alternately and repeatedly.

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