Reactor

Abstract

This specification discloses a reactor, a reaction method using the reactor, and uses of the reactor. The reactor can solve the coking problem that can occur during the synthesis gas production process without applying a costly and energy-intensive method of introducing excessive amounts of steam or carbon dioxide. The reactor can also achieve the above objectives in a DRM process that does not use steam. This specification also discloses a reaction method using the reactor and uses of the reactor.

Description

[Technical Field]

[0001] This application claims the benefit of priority based on Korean Patent Application No. 10-2022-0140787, dated October 27, 2022, the entire contents of which are incorporated herein by reference.

[0002] This specification discloses a reactor, a reaction method using said reactor, and uses of said reactor. [Background technology]

[0003] Syngas is known in the industry as a gas mixture containing hydrogen (H2) and carbon monoxide (CO). Syngas is typically produced from raw materials such as coal, heavy oil, naphtha, and / or natural gas, for example, by reforming natural gas.

[0004] The most well-known processes for producing synthetic gas from natural gas are the SMR (Steam Methane Reforming) process and the CDR (Carbon Dioxide Reforming) process. Unlike the SMR process, the CDR process does not use steam, so it is also called the DRM (Dry Reforming of Methane) process.

[0005] The key reaction of the SMR process is shown in the following reaction scheme 1, and the key reaction of the DRM process is shown in the following reaction scheme 2, both of which are endothermic reactions.

[0006] [Reaction Scheme 1] CH4+H2O→3H2+CO, △H=206.28kJ / mol

[0007] [Reaction Scheme 2] CH4+CO2→2H2+2CO, △H=247.44kJ / mol

[0008] Catalysts are commonly used in SMR and DRM processes.

[0009] However, during the reaction process, the raw material (such as natural gas) is reformed, generating residual carbon called coke, which can reduce the activity of the catalyst, a problem known as coking.

[0010] There are various causes of coking, including the so-called Boudouard reaction.

[0011] The Boudouard reaction is a reaction in which carbon monoxide generated during the reaction process dissociates at a relatively low temperature to form coke, as shown in Reaction Scheme 3 below. This reaction is known to occur normally at temperatures below about 700°C.

[0012] [Reaction Scheme 3] 2CO(g) → C(s) + CO2(g)

[0013] Both the SMR and DRM processes are endothermic reactions, but if there is a region within the reaction zone where the reaction rate is relatively fast, the temperature in that region will drop compared to the ambient temperature, and the Boudouard reaction may be accelerated in that region. This region where the temperature drops compared to the ambient temperature is also called a cold spot.

[0014] Generally, the reaction rate tends to decrease as the reaction passes through the low temperature point within the reaction zone. The heat applied in this region where the reaction rate is reduced can decompose the reactant or raw material, and this decomposition can also cause the coking phenomenon. For example, the raw material methane (CH4) can produce coke at high temperatures of about 850°C or higher according to the following reaction formula 4:

[0015] [Reaction Scheme 4] CH4 → C(s) + 2H2(g)

[0016] Non-Patent Document 1 discloses a method for preventing coking in the SMR process by introducing an excess amount of steam.

[0017] The DRM process is classified as a carbon capture technology because it uses carbon dioxide as a material, but because it does not use water vapor, it cannot prevent coking by introducing water vapor.

[0018] Non-Patent Document 2 discloses the use of an excess amount of carbon dioxide in the DRM process to prevent coking, but the method disclosed in Non-Patent Document 2 is a costly method with high energy consumption. [Prior art documents] [Non-patent literature]

[0019] [Non-Patent Document 1] Bak, YC and Cho KJ, “Status for the Technology of Hydrogen Production from Natural Gas,” Korean Chem. Eng. Res., Vol. 43, No. 3, June, 2005, pp. 344-351 [Non-patent document 2] Armor, JN, “The Multiple Roles for Catalysis in the Production of H2,” Applied Catalysis, A:General, 176, 159-176 (1999) Summary of the Invention [Problem to be solved by the invention]

[0020] This specification discloses a reactor, a reaction method using the reactor, and uses of the reactor. The purpose of this specification is to disclose a reactor that can solve the coking problem that can occur in the process of producing synthesis gas without applying a method that requires the introduction of excessive amounts of steam or carbon dioxide, which is expensive and consumes a lot of energy.

[0021] The purpose of this specification is to disclose a reactor that can achieve the above objectives in a DRM process that does not use steam, without using a costly and energy-intensive method.

[0022] The purpose of this specification is to disclose a reaction method using said reactor and the use of said reactor. [Means for solving the problem]

[0023] Among the physical properties mentioned in this specification, those whose results are affected by the measurement temperature are physical properties measured at room temperature unless otherwise specified.

[0024] Room temperature means a natural temperature that is neither heated nor cooled. For example, room temperature may be any temperature within the range of 10°C to 30°C, and may be a temperature of about 23°C or about 25°C. The unit of temperature referred to in this specification is Celsius (°C) unless otherwise specified.

[0025] As referred to in this specification, the temperature of a pipeline, internal passage, catalytic section or non-catalytic section or the internal temperature of a pipeline, internal passage, catalytic section or non-catalytic section means the temperature at the center of said pipeline, internal passage, catalytic section or non-catalytic section, unless otherwise specified.

[0026] The core temperature is the temperature at the center of gravity of the cross section of the pipeline, internal passage, catalytic section or non-catalytic section. For example, referring to FIG. 7, the core temperature of the pipeline is T Center Referring to FIG. 7, the characteristic points (P T ) the center of gravity of the cross section of the pipeline 100 can be identified, and the temperature T measured at the center of gravity Center the specific point (P T ) can be said to be the central temperature.

[0027] Among the physical properties mentioned in this specification, those whose results are affected by measurement pressure are physical properties measured at normal pressure unless otherwise specified.

[0028] The term "normal pressure" refers to both pressurized and unpressurized natural pressure. For example, normal pressure may refer to approximately 1 atmosphere, which is the normal atmospheric pressure level.

[0029] Thermodynamic properties referred to herein are measured at 25° C. and 1 atmosphere pressure unless otherwise specified.

[0030] Among the physical properties mentioned in this specification, those whose results are affected by the humidity used for measurement are those measured at standard humidity unless otherwise specified.

[0031] Standard humidity is usually relative humidity, and means a humidity of about 60% to 65%.

[0032] Among the terms used in this specification, the term "a to b" that specifies a range means a range between a and b, including a as the lower limit and b as the upper limit.

[0033] This specification discloses a reactor. The term reactor refers to a device capable of carrying out any reaction. In one embodiment, the reaction may include an endothermic reaction. In one embodiment, the reaction may be a steam methane reforming (SMR) process reaction or at least a portion of the steam methane reforming (SMR) process reaction. In another embodiment, the reaction may be a dry reforming of methane (DRM) process reaction or at least a portion of the dry reforming of methane (DRM) process reaction.

[0034] The reactor may be a syngas production apparatus or a part of the syngas production apparatus, and the syngas production apparatus may be an apparatus in which a dry reforming of methane (DRM) process is performed.

[0035] Hereinafter, the reaction apparatus and the like will be described with reference to the drawings according to the examples, but the scope of the reaction apparatus and the like is not limited to the following.

[0036] FIG. 1 is an illustration of an exemplary reactor 10.

[0037] The reactor 10 may include at least one pipeline 100. The pipeline 100 may include an internal passage formed to allow a fluid to flow. The shape of the pipeline 100 is not particularly limited, and may be designed taking into account the physical and / or chemical properties of the fluid to be reacted.

[0038] Figure 2 shows an exemplary configuration of the pipeline 100 of the reactor 10. The reactor 10 of Figure 1 includes a pipeline 100 formed in a "single" shape. The pipeline 100 may have a configuration in which U-shapes are repeated as shown in Figure 2(a), or may be U-shaped as shown in Figure 2(b), or may have a configuration in which U-shaped pipelines 100 are repeated and staggered so as not to overlap each other as shown in Figure 2(c).

[0039] There is no particular limitation on the cross-sectional shape of the pipeline 100. The cross-sectional shape of the pipeline 100 may be appropriately designed taking into consideration the physical and / or chemical properties of the fluid to be reacted. FIG. 3 shows an exemplary cross-sectional shape of the pipeline 100. The pipeline may have a surface that forms the internal passage. FIG. 3 shows the cross-sectional shape of a pipeline having the surface 110 and the internal passage 120. As shown in FIG. 3, the cross-section of the pipeline may generally be circular or rectangular. In addition, the cross-sectional shape may be various shapes such as a triangle, a rhombus, a parallelogram, or an ellipse.

[0040] The internal passage of the pipeline may be a space formed to allow a fluid to flow. The surface of the pipeline (110 in FIG. 3) may serve as a medium for transferring thermal energy to the internal passage by a heating unit (described later). In this case, the surface may be formed of a material having suitable thermal conductivity and high heat resistance. The surface may be a material that generates so-called resistive Joules or Joule heat when an electric current flows through it. A typical example of such a material may be an alloy containing nickel and chromium, but is not limited thereto.

[0041] The pipeline 100 of the reactor 10 may have an appropriate length in consideration of the physical and / or chemical properties of the fluid to be reacted.

[0042] In the reactor 10, the internal passage 120 of the pipeline 100 may be formed to allow fluid to flow in any one direction. For example, the pipeline may be formed to allow the fluid to flow in one direction by gravity, or the reactor may be formed to allow fluid flow to be induced by an external force such as a pump, and both gravity and external force may be applied.

[0043] The reactor may include a plurality of heating units, which may be included in the reactor to transfer thermal energy to the fluid flowing through the internal passage in at least a portion of the pipeline.

[0044] The plurality of heating units may be installed so as to be able to independently transfer heat energy to the internal passage, i.e., at least some of the plurality of heating units are installed so as to be able to independently determine the amount of heat transferred to the internal passage without being affected by other heating units.

[0045] Therefore, the pipeline 100 of the reactor 10 can be divided into two or more heating zones 130 along the fluid flow direction DF. As used herein, the term fluid flow direction DF refers to the direction of fluid flow in the internal passage 120 of the pipeline 100. In FIG. 1, the pipeline is configured so that fluid flows from point (A) to point (B). In this case, the direction from point (A) to point (B) is the fluid flow direction DF.

[0046] In this specification, the term "fluid" refers to a substance that can flow, and is a general term that refers to gas, liquid, plasma, and the like.

[0047] In the DRM process, the fluid may contain at least carbon dioxide.

[0048] The fluid may also contain an organic hydrocarbon compound. As used herein, the term "organic hydrocarbon compound" refers to a hydrocarbon or a compound in which at least some of the carbon atoms of the hydrocarbon are replaced with oxygen (O), nitrogen (N), sulfur (S), and / or halogens (F, Cl, Br, and / or I), or at least some of the carbon atoms of the hydrocarbon are bonded to oxygen (O), nitrogen (N), sulfur (S), and / or halogens (F, Cl, Br, and / or I). Examples of organic hydrocarbon compounds include, but are not limited to, methane, ethane, and propane. In the DRM process, the organic hydrocarbon compound may include at least some of the compounds that make up natural gas, particularly methane (CH4). The fluid may be or contain a reactant that reacts with thermal energy from the heating unit. For example, if the fluid contains carbon dioxide and an organic hydrocarbon compound, they can react. Through this reaction, so-called synthesis gas containing hydrogen and carbon monoxide can be produced.

[0049] The fluid used in the DRM process may be substantially free of water (e.g., steam). Steam refers to the vapor form of water (H2O). "Substantially free of water" in the fluid means that water is not intentionally present in the fluid. For example, even if a small amount of water is naturally present, the fluid can be considered to be substantially free of water as long as the content is below a certain level.

[0050] For example, the upper limit of the water content in the fluid may be about 10 wt%, 9 wt%, 8 wt%, 7 wt%, 6 wt%, 5 wt%, 4 wt%, 3 wt%, 2 wt%, 1 wt%, 0.5 wt%, 0.1 wt%, 0.05 wt%, 0.01 wt%, 0.005 wt%, 0.001 wt%, or 0.0001 wt%, based on the total weight of the fluid, and the lower limit may be about 0 wt%. The water content may be within a range equal to or less than any one of the above upper limits; or within a range equal to or less than any one of the above upper limits but equal to or greater than any one of the above lower limits. The fluid may also be substantially free of water in both solid and liquid phases, such as ice or liquid water.

[0051] 1 shows a plurality of heating zones 130 formed by the plurality of heating units. A heating zone is a zone to which thermal energy is transferred by the heating unit. The heating unit can transfer thermal energy to the heating zones 130 by conduction, convection, and / or radiation.

[0052] The reactor 10 of Figure 1 includes two or more heating zones 130a, 130b, 130c, and 130d formed by a plurality of heating units 200, 210, 220, 230, and 240. The amount of heat energy transferred to each heating zone 130 can be determined independently by the plurality of heating units 200.

[0053] For example, the heating region 130 may be a region that receives thermal energy directly from the heating unit 200. Such a region may be i) the internal passage 120 of the pipeline 100 if the heating unit 200 is part of the pipeline 100, or ii) the internal passage 120 of a portion of the pipeline 100 located closest to the external heat source if the heating unit 200 is an external heat source installed apart from the pipeline 100. FIG. 4 is an exemplary diagram of a pipeline 100 for explaining the heating region 130. Referring to FIG. 4(a), if the heating unit 200 is a portion of the pipeline 100 (the surface of the pipeline) that generates so-called resistance Joules or Joule heat when electricity is applied, the internal passage 120 of the pipeline 100 that generates the resistance Joules or Joule heat may be the heating region 130a. 4(b), if the heating unit 200 is an external heat source 230 spaced apart from the pipeline 100, the internal passage 120 of the pipeline 10 closest to the external heat source (i.e., vertical distance in FIG. 4(b)) may be the heating region 130c. Referring to FIG. 1, additional examples of heating regions 130a, 130b, 130c, and 130d generated corresponding to each heating unit 200 can be seen.

[0054] The internal passage 120 of the exemplary reactor 10 may include an unheated region. When the pipeline 100 is divided into two or more heated regions 130 by multiple heating units, a region that does not correspond to the heated region 130, i.e., a region of the internal passage 120 that does not substantially receive thermal energy from the heating unit 200, may be the unheated region. However, even in an unheated region, thermal energy may be indirectly transferred by a heated fluid or an adjacent heating unit.

[0055] The heating zones 130 of the reactor 10 may be independently supplied with thermal energy by a plurality of heating units. The thermal energy supplied to each heating zone 130 may be transferred to the fluid flowing through the internal passages 120, thereby heating the fluid. In this process, the fluid is heated by transferring thermal energy to the fluid, which generally results in an increase in the temperature of the fluid.

[0056] In the reactor 10, two or more heating zones are formed along the fluid flow direction, and the amount of thermal energy transferred to each heating zone can be independently controlled. This allows for optimizing the temperature profile in the internal passages, thereby preventing problems such as coking (e.g., a decrease in catalytic activity).

[0057] At least some or all of the heating units may be so-called electric heating units, which are units that can generate heat from electricity. Such units have relatively free temperature adjustment, which allows for more precise control of the temperature profile in the internal passage.

[0058] Such an electric heating unit can generate heat through direct current or alternating current. When the electric heating unit is supplied with electric energy, the electric energy can be supplied by connecting a power supply 300 directly or indirectly to the heating unit 200. If the power supply 300 is a DC power supply, DC is supplied to the heating unit 200, and if the power supply 300 is an AC power supply, AC is supplied to the heating unit 200. The reaction device 10 can use a DC power supply or an AC power supply as needed.

[0059] As is well known, DC is a current that flows in a constant direction independent of time, while AC is a current whose magnitude and phase change periodically with time. A DC power supply can provide a voltage that is independent of time, while an AC power supply can provide a voltage whose magnitude and phase change periodically with time.

[0060] The electric heating unit may be a direct electric heating unit, an indirect electric heating unit, or an induction heating unit. A direct electric heating unit generates heat by directly supplying electricity to a heating target. For example, the electric heating unit may be a pipeline or the surface of the pipeline that generates resistance Joule or Joule heat when electricity is passed through it. Direct current or alternating current may be directly applied to the pipeline or surface to generate heat through resistance Joule or Joule heat. The direct current and alternating current may be supplied by the power supply 300, as described above, being electrically connected directly or indirectly to a portion of the pipeline 100.

[0061] In this way, when the heating unit 210 is a pipeline or its surface that generates heat by passing electricity, the power supply device 300 may be electrically connected to at least a portion of the pipeline 100 or its surface. The pipeline 100 or its surface 110 electrically connected to the power supply device 300 can generate heat by receiving electrical energy from the power supply device 300. This heat can be transferred to the fluid flowing through the internal passage 120.

[0062] In this case, the pipeline or its surface may be made of a material that has excellent thermal conductivity, is heat-resistant, and allows the flow of electrical current while generating so-called resistive Joule or Joule heat in order to efficiently transfer thermal energy to the fluid in the pipeline, such as, but not limited to, nickel, chromium, and / or alloys containing nickel and chromium.

[0063] 1 illustrates the heating zone 130a formed by the electric direct heating unit 210. AC or DC electricity is supplied from a power supply 300 to the surface 110 of the pipeline 100, causing the surface 110 to generate heat, which can be contained in the heating zone 130a and transferred to the fluid flowing through the internal passage 120. The amount of heat can be adjusted by adjusting the amount of electricity supplied by the power supply 300.

[0064] The electric indirect heating unit is a unit that transfers heat generated by electricity back to the heating area, rather than directly generating heat in the heating area. Such an electric indirect heating unit may be an external heat source (410 in FIG. 1) separated from the pipeline 100. The external heat source 410 can independently generate heat energy from electrical energy. The heat energy generated by such an external heat source is transferred to the pipeline 100 to heat the fluid flowing through the internal passage 120.

[0065] The external heat source 410 may be electrically connected directly or indirectly to the power supply 300 to receive electrical energy. The power supply 300 may be a DC power supply or an AC power supply. Resistance Joules or Joule heat is generated in the external heat source 410 by the electrical energy supplied through the power supply 300, and this heat is transferred to the heating region 130b and can heat the fluid flowing through the internal passage 120. The amount of heat can be adjusted by adjusting the amount of electrical energy supplied by the power supply 300.

[0066] The exemplary reactor 10 of FIG. 1 shows a heating zone 130b to which heat generated by the electric indirect heating unit 410 is transferred. The external heat source 410 may be installed at a distance from the pipeline 100 so as to transfer thermal energy to all surfaces of the pipeline 100 corresponding to the heating zone 130b. For example, the external heat source 410 may be provided in a form surrounding the pipeline 100 so as to transfer thermal energy to all surfaces of the pipeline 100 corresponding to the heating zone 130b. The structure capable of transferring thermal energy to all surfaces of the pipeline 100 is not limited to the above. This method can prevent thermal energy from being transferred locally to only a specific portion of the fluid flowing through the heating zone 130b.

[0067] An induction heating unit can perform heating through induction current. For example, the induction heating unit can be a pipeline or its surface that generates resistance joule or Joule heat through induction current. For example, as illustrated in FIG. 1 , such an induction heating unit can be formed by applying electricity such as alternating current to a coil wire 500 that is spirally arranged around the pipeline 100 and spaced apart from it. The coil wire 500 can be spirally arranged around the pipeline 100 corresponding to the heating region 130d and spaced apart from it. The coil wire 500 can be connected to a power supply 300 to pass current such as alternating current through it, and the power supply 300 can be an AC power supply that applies alternating current. When an alternating current is applied to the coil wire 500, an induced current is generated on the surface 110 of the pipeline 100 due to electromagnetic induction. The generated induced current generates resistance Joules or Joule heat on the surface 110 of the pipeline 100, and the generated resistance Joules or Joule heat is transferred to the heating region 130d to heat the fluid flowing in the internal passage 120 of the pipeline 100.

[0068] In this case, the pipeline 100 or its surface 110 may be made of a material that generates resistance Joules or Joule heat due to an induced current generated by the coil wire 500. For example, the pipeline 100 or its surface 110 may be made of a material such as, but not limited to, nickel, chromium, or an alloy containing nickel and chromium. The strength or degree of the resistance Joules or Joule heat can be adjusted by adjusting the amount of electrical energy supplied by the power supply unit 300. In this case, the strength of the induced current can also be adjusted by changing the number of turns of the coil wire 500, the predetermined distance from the pipeline 100, and / or the material of the coil wire 500.

[0069] Such electrical heating units can be more precisely adjusted with relative freedom to produce heat, thereby allowing for more precise control of the temperature profile within the internal passageway.

[0070] The heating unit may include only the electric heating unit, or a traditional heating unit may be used if necessary. For example, the heating unit 230 that may be included in the reactor 10 may include an external heat source 420 that is installed separately from the pipeline 100 and converts fossil energy into thermal energy. The thermal energy converted by the external heat source is transferred to the pipeline 100 to heat the fluid flowing in the internal passage 120 of the pipeline 100. The external heat source 420 may generate thermal energy using coal, oil, or other fuels as raw materials. The generated thermal energy may be accommodated in the heating region 130c and transferred to the fluid flowing in the internal passage 120. The intensity of the thermal energy may be adjusted by adjusting the amount of raw material injected.

[0071] Referring to FIG. 1, at least one heating unit 230, which is one of the predetermined methods for generating thermal energy to be transmitted to the heating region 130c, is an external heat source 420 installed separately from the pipeline 100. The external heat source 420 may be configured to convert fossil fuels into thermal energy. The external heat source 420 may be installed separately from the pipeline 100 so as to transmit thermal energy to all surfaces of the pipeline 100 corresponding to the heating region 130c. For example, the external heat source 420 may be installed in a form surrounding the pipeline 100 so that thermal energy is directly transmitted to all surfaces of the pipeline 100 corresponding to the heating region 130c. However, the configuration is not limited to this as long as thermal energy can be transmitted to all surfaces of the corresponding pipeline 100. Configuring the external heat source 420 so that thermal energy is transmitted to all surfaces of the pipeline 100 corresponding to the heating region 130c prevents uneven heating due to thermal energy being transmitted only to specific locations in the fluid flowing through the heating region 130c.

[0072] The pipeline may include a catalyst section. Such a catalyst section may exist in the internal passage. The term catalyst section refers to the region of the internal passage where a catalyst is present. Figure 5 shows an example of a reactor 10 including a catalyst section 600 formed by filling the internal passage of the pipeline 100 with a catalyst 610. As fluid passes through the catalyst section 600, a target reaction may occur.

[0073] The catalyst may be appropriately selected in consideration of the target reaction. For example, a known endothermic reaction catalyst may be used for the reforming reaction described above. An endothermic reaction catalyst is a catalyst that catalyzes an endothermic reaction. Examples of such catalysts include known DRM reaction catalysts, such as nickel catalysts and / or noble metal (e.g., Rh, Ru, and Pt) catalysts, but are not limited thereto.

[0074] The length of the catalyst section can be controlled according to the purpose. For example, the length L C The length L of the pipeline P Ratio to L C / L P For example, the ratio L C / L P The lower limit of the ratio L may be about 0.3, 0.35, 0.4, 0.45, 0.5, 0.55, 0.6, 0.65, 0.7, 0.75, or 0.8, and the upper limit may be about 1, 0.95, 0.9, 0.85, 0.8, 0.75, 0.7, or 0.65. C / L P may be in a range that is equal to or greater than any one of the aforementioned lower limits; equal to or less than any one of the aforementioned upper limits; or equal to or greater than any one of the aforementioned lower limits but equal to or less than any one of the aforementioned upper limits.

[0075] The catalyst section may be provided continuously along the fluid flow direction. That is, the catalyst section may be a continuous catalyst section. A continuous catalyst section refers to a case where a catalyst is present throughout the catalyst section. For example, if there is no section without a catalyst between the point where the fluid first contacts the catalyst and the point where the fluid last contacts the catalyst in the pipeline along the fluid flow direction, this case may be a continuous catalyst section. An example of such a continuous catalyst section is shown in FIG. 5.

[0076] On the other hand, the example shown in Figure 6 is a discontinuous catalyst section. For example, if there is a section without catalyst between the point where the fluid first comes into contact with the catalyst and the point where the fluid last comes into contact with the catalyst in the pipeline along the fluid flow direction, it can be a discontinuous catalyst section. Figure 6 illustrates an example of such a discontinuous catalyst section 600, where when any one point (P1) and any other point (P2) are selected within the catalyst section 600, there is a portion (P3) without catalyst between them.

[0077] The pipeline 100 of the reactor 10 may include a catalytic section 600 and a non-catalytic section 700 (FIG. 5). That is, the reactor 10 has the above-mentioned ratio L C / L P If the above condition is satisfied, the catalyst section may include only a catalyst section, or may also include a non-catalytic section in which no catalyst is present.

[0078] For example, as shown in FIG. 5, the pipeline 100 may include a non-catalytic section 700 and a catalytic section 600 in sequence along the fluid flow direction DF.

[0079] With this configuration, in the reaction process described below, the fluid can be configured to first enter the non-catalytic section 700 and then enter the catalytic section 600. This method can prevent excessive environmental changes (e.g., temperature and / or pressure changes) that may occur during the reaction due to the high partial pressure and high concentration of the reactant contained in the fluid. As illustrated in Figures 5 and 6, forming the non-catalytic section 700 after the catalytic section 600 can also prevent excessive environmental changes (e.g., temperature and / or pressure changes) caused by reaction products.

[0080] In this specification, in the above case, the non-catalytic section 700 located before the catalytic section 600 along the fluid flow direction DF is referred to as the first non-catalytic section, and the non-catalytic section 700 located after the catalytic section 600 is referred to as the second non-catalytic section.

[0081] The total length of the pipeline 100 (L P ) can be appropriately designed depending on the type of reaction target substance, the amount of inflow, etc., and is not particularly limited. For example, P The lower limit of the length L may be about 5 m, 6 m, 7 m, 8 m, 9 m, 11 m, or 12 m, and the upper limit may be about 100 m, 90 m, 80 m, 70 m, 60 m, 50 m, 40 m, 30 m, 20 m, 19 m, 18 m, 17 m, 16 m, 15 m, 14 m, 13 m, 12 m, 11.9 m, 11.8 m, 11.7 m, 11.6 m, 11.5 m, 11.4 m, 11.3 m, or 11.2 m.P may be in a range that is equal to or greater than any one of the aforementioned lower limits; equal to or less than any one of the aforementioned upper limits; or equal to or greater than any one of the aforementioned lower limits but equal to or less than any one of the aforementioned upper limits.

[0082] For example, the length L of the first non-catalytic section NC1 The length L of the pipeline P Ratio to L NC1 / L P The lower limit of the ratio L may be about 0.01, 0.05, 0.1, 0.3, 0.5, 0.7, or 0.9, and the upper limit may be about 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.28, 0.26, 0.24, 0.22, or 0.2. NC1 / L P may be in a range that is equal to or greater than any one of the aforementioned lower limits; equal to or less than any one of the aforementioned upper limits; or equal to or greater than any one of the aforementioned lower limits but equal to or less than any one of the aforementioned upper limits.

[0083] The length (L) of the second non-catalytic section of the pipeline 100, if present NC2 ) is the length (L NC1 ) and the length of the catalyst section 600 (L C ) is determined, the length of the first non-catalytic section (L NC1 ) and the length of the catalyst section 600 (L C ) can be subtracted from the length.

[0084] The catalyst 610 in the catalyst section 600 of the reactor 10 may be uniformly distributed throughout the catalyst section 600 or may be non-uniformly distributed.

[0085] In the catalyst section 600 of the reactor 10, the catalyst 610 may be formed in a fluidized bed or a fixed bed.

[0086] In the exemplary reactor 10, the catalyst section 600 may be divided into a reaction initiation section 600a and a reaction continuation section 600b. The reaction initiation section 600a may extend, for example, from the point where the catalyst section 600 begins along the fluid flow direction DF to the point where the internal temperature is lowest within 50% of the length of the catalyst section 600. The reaction continuation section 600b may extend from the point in the catalyst section 600 where the reaction initiation section 600a ends to the point where the catalyst section 600 ends.

[0087] Referring to FIG. 8, at a point 1 / 2L, which is 50% of the length of the catalyst section 600 along the fluid flow direction DF, C As described above, the reaction initiation section 600a is 1 / 2 L from the point where the catalyst section 600 starts. C The point with the lowest central temperature within the range (e.g., T L The reaction continuation section 600b may be up to the point T L to the point where the catalyst section 600 ends.

[0088] In the reactor 10, the non-catalytic section 700, the reaction initiation section 600a, and the reaction continuation section 600b each have at least one heating zone 130, and the heating zones 130 can be independently transferred with thermal energy. The manner of transferring the thermal energy can be seen from the above.

[0089] In the exemplary reactor 10, one of the one or more heating zones 130 in the reaction initiation section 600a may receive the highest thermal energy transfer among the heating zones 130 in the entire pipeline 100. The reactor 10 can perform precise temperature control so that one of the one or more heating zones 130 in the reaction initiation section 600a receives the highest thermal energy transfer among the heating zones 130 in the entire pipeline 100 to minimize conditions for the occurrence of coking.

[0090] The temperature control in the reactor 10 prevents the formation of cold spots, considering that the core reaction is an endothermic reaction, and even if a cold spot does form, it can prevent the temperature from dropping to a level that would cause coking. Furthermore, the temperature control can prevent a sudden temperature rise due to a decrease in the reaction rate of the reactants. That is, the reactor 10 can provide a reactor that prevents a decrease in catalytic activity by preventing the formation of conditions that induce the formation of carbon residue due to the Boudouard reaction and the self-decomposition of organic hydrocarbon compounds in the fluid.

[0091] That is, the heating unit of the reactor may be installed so that the catalyst zone includes a stabilization zone above a certain level. The term "stabilization zone" may refer to a region within the catalyst zone that is controlled so that no substantial temperature change occurs during the reaction.

[0092] For example, the stabilization interval may refer to a region where ΔT1 in the following equation 3 is below a certain level.

[0093] [Formula 3] △T1=T S / T CA ×100

[0094] In Equation 3, T CA is the average temperature in the stabilization section, and T S is the temperature T at any point within the stabilization section i and the aforementioned T CA is the absolute value of the difference between

[0095] The upper limit of ΔT1 in Equation 3 in the stabilization section may be about 10%, 9%, 8%, 7%, 6%, 5%, 4%, 3%, 2%, 1.8%, 1.6%, 1.4%, 1.2%, 1%, 0.8%, 0.6%, 0.4%, 0.2%, or 0.1%, and the lower limit may be about 0%, 0.01%, 0.05%, 0.1%, or 0.15%. ΔT1 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. By forming such a stabilization section within the catalyst section, problems such as coking can be solved.

[0096] For example, the reaction continuation section can be the stabilization section. CA is the average temperature for the section from the point at which the catalyst section 600 is 50% of its length to the point at which the catalyst section 600 ends. The average temperature is the average of the central temperatures mentioned at the beginning of this specification. Also, in Equation 3, T S is the above T CA T is the central temperature at any one point in the section from the point that is 50% of the length of the catalyst section 600 where the temperature was measured to the point where the catalyst section 600 ends. i and the aforementioned T CA For the central temperature at any one point, ΔT1 according to Equation 3 can satisfy the above range regardless of which point is selected from the section from the 50% point of the catalyst section 600 to the end point of the catalyst section 600.

[0097] For example, the length L of the stabilization section formed in the catalyst section S The length L of the catalyst section C Ratio to L S / L CThe lower limit of the ratio L may be about 0.2, 0.25, 0.3, 0.35, 0.4, 0.45, or 0.5, and the upper limit may be about 1, 0.95, 0.9, 0.85, 0.8, 0.75, 0.7, 0.65, 0.6, or 0.55. S / L C may be in the range of less than or equal to any one of the aforementioned upper limits; or may be in the range of less than or equal to any one of the aforementioned upper limits, but greater than or equal to or greater than any one of the aforementioned lower limits.

[0098] T in the above formula 3 CA The lower limit of the temperature T may be about 750°C, 760°C, 770°C, 780°C, 790°C, 800°C, 805°C, 810°C, 815°C, 820°C, 825°C, or 830°C, and the upper limit may be about 1,000°C, 950°C, 900°C, 850°C, 845°C, 840°C, or 835°C. CA may be in a range that is equal to or greater than any one of the aforementioned lower limits; equal to or less than any one of the aforementioned upper limits; or equal to or greater than any one of the aforementioned lower limits but equal to or less than any one of the aforementioned upper limits.

[0099] The reactor, pipeline, or heating unit may be installed so as to satisfy the following formula 5, thereby further suppressing the occurrence of problems such as coking.

[0100] [Formula 5] T NCA ≧T CL

[0101] In Equation 5, T NCA is the average temperature of the non-catalytic section, and T CL is the minimum temperature observed within the catalyst section. CL For example, T may be the point at which the temperature is lowest within 50% of the length of the catalytic section. For example, if there are multiple non-catalytic sections 700, T in Equation 5 NCAmay be the average value of the temperatures of all non-catalytic sections 700.

[0102] In relation to Equation 5, T in Equation 5 NCA T CL Ratio to T NCA / T CL The lower limit may be about 1, 1.01, 1.02, 1.03, or 1.04, and the upper limit may be about 5, 4, 3, 2, 1.9, 1.8, 1.7, 1.6, 1.5, 1.4, 1.3, 1.2, 1.1, 1.09, 1.08, 1.07, 1.06, or 1.05. The ratio may be in a range that is greater than or equal to any one of the lower limits mentioned above; less than or equal to any one of the upper limits mentioned above; or greater than or equal to any one of the lower limits mentioned above but less than or equal to any one of the upper limits mentioned above.

[0103] The reactor, pipeline, or heating unit may be installed so that the following formula 6 is satisfied, thereby further suppressing problems such as the occurrence of coking.

[0104] [Formula 6] T NCH ≧T CH

[0105] In Equation 6, T NCH is the highest temperature in the non-catalytic section, and T CH means the highest temperature in the catalyst section. For example, T in Equation 6 NCH Specifically, the temperature may be the highest core temperature in the first non-catalytic section.

[0106] In relation to Equation 6, T in Equation 6 NCH T CH Ratio to T NCH / T CHThe lower limit may be about 1, 1.01, 1.02, 1.03, or 1.04, and the upper limit may be about 5, 4, 3, 2, 1.9, 1.8, 1.7, 1.6, 1.5, 1.4, 1.3, 1.2, 1.1, 1.09, 1.08, 1.07, 1.06, or 1.05. The ratio may be in a range that is greater than or equal to any one of the lower limits mentioned above; less than or equal to any one of the upper limits mentioned above; or greater than or equal to any one of the lower limits mentioned above but less than or equal to any one of the upper limits mentioned above.

[0107] The reactor, pipeline, or heating unit may be configured so that the absolute value of ΔR3 in the following formula 7 is within a certain range, thereby more effectively achieving the desired effect.

[0108] [Formula 7] △R3=(T NCA -T CA ) / T CA ×100

[0109] In Equation 7, T CA is the average temperature in the stabilization section, and T NCA is the average temperature of the non-catalytic section.

[0110] The upper limit of the absolute value of ΔR3 may be approximately 20%, 18%, 16%, 14%, 12%, 10%, 8%, 6%, 4%, 2%, 1.9%, 1.8%, 1.7%, or 1.6%, and the lower limit may be approximately 0%, 0.5%, 1%, or 1.5%. The absolute value of ΔR3 may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. ΔR3 may be a negative or positive number.

[0111] The reactor, pipeline, or heating unit may be configured so that the absolute value of ΔR4 in the following formula 8 is within a certain range, thereby more effectively achieving the desired effect.

[0112] [Formula 8] △R4=(T CH -T CA ) / T CA ×100

[0113] T in Equation 8 CA is the average temperature in the stabilization section, and T CH is the maximum temperature in the catalyst section.

[0114] The upper limit of the absolute value of ΔR4 may be approximately 20%, 18%, 16%, 14%, 12%, 10%, 8%, or 6%, and the lower limit may be approximately 0%, 0.5%, 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, or 5.5%. The absolute value of ΔR4 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. ΔR4 may be a positive number.

[0115] The reactor, pipeline, or heating unit may be configured so that the absolute value of ΔR5 in the following formula 9 is within a certain range, thereby more effectively achieving the desired effect.

[0116] [Formula 9] △R5=(T CL -T CA ) / T CA ×100

[0117] In Equation 9, T CA is the average temperature in the stabilization section, and T CL is the minimum temperature in the catalyst section.

[0118] The upper limit of the absolute value of ΔR5 may be approximately 20%, 18%, 16%, 14%, 12%, 10%, 8%, or 6%, and the lower limit may be approximately 0%, 0.5%, 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, or 5.5%. The absolute value of ΔR5 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. ΔR5 may be a negative number.

[0119] The reactor, pipeline, or heating unit may be configured so that the absolute value of ΔR6 in the following formula 10 is within a certain range, thereby more effectively achieving the desired effect.

[0120] [Formula 10] △R6=(T NCH -T CA ) / T CA ×100

[0121] T in Equation 10 CA is the average temperature in the stabilization section, and T NCH is the maximum temperature in the non-catalytic section.

[0122] The upper limit of the absolute value of ΔR6 may be approximately 20%, 18%, 16%, 14%, 12%, 10%, 8%, or 6%, and the lower limit may be approximately 0%, 0.5%, 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, or 5.5%. The absolute value of ΔR6 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. ΔR6 may be a positive or negative number.

[0123] The reactor, pipeline, or heating unit may be configured so that the absolute value of ΔR7 in the following formula 11 is within a certain range, thereby more effectively achieving the desired effect.

[0124] [Formula 11] △R7=(T CL -T CA ) / T CA ×100

[0125] T in Equation 11 CA is the average temperature in the stabilization section, and T HCL is the minimum temperature in the non-catalytic section.

[0126] The upper limit of the absolute value of ΔR7 may be approximately 20%, 18%, 16%, 14%, or 12%, and the lower limit may be approximately 0%, 0.5%, 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5%, 5%, 5.5%, 6%, 6.5%, 7%, 7.5%, 8%, 8.5%, 9%, 9.5%, 10%, 10.5%, or 11%. The absolute value of ΔR7 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. ΔR7 may be a positive or negative number.

[0127] The installation configuration of the heating unit can be adjusted to enable the reactor to be driven in this manner.

[0128] For example, the heating unit may be installed so that R1 in the following formula 1 falls within a predetermined range.

[0129] [Formula 1] R1=L C / H I

[0130] In Equation 1, L C is the length of the catalyst section, and HI is the average spacing between the heating units. C and H I have the same units.

[0131] The upper limit of R1 in Formula 1 may be about 100, 95, 90, 85, 80, 75, 70, 65, 60, 55, 50, 45, 40, 35, 30, 25, 20, 15, 10, 9, 8, 7, 6, or 5.5, and the lower limit may be about 0.5, 1, 1.5, 2, 2.5, 3, 3.5, 4, 4.5, or 5. R1 may be within a range that is greater than or equal to any one of the lower limits mentioned above; less than or equal to any one of the upper limits mentioned above; or greater than or equal to or exceeding any one of the lower limits mentioned above, but less than or equal to any one of the upper limits mentioned above.

[0132] As long as the above conditions are satisfied, the intervals between the heating units may be constant or may vary. For example, the upper limit of the standard deviation of the intervals between the heating units may be about 10, 9, 8, 7, 6, 5, 4, 3, 2, 1, 0.5, or 0.1, and the lower limit may be about 0, 0.1, or 0.5. The standard deviation may be within a range that is equal to or exceeds any one of the lower limits; that is equal to or exceeds any one of the upper limits; or that is equal to or exceeds any one of the lower limits but equal to or exceeds any one of the upper limits. For example, if there are four heating units and there are three intervals (L1, L2, L3) between them, and the average of the intervals is A, the standard deviation may be expressed as [{(A-L1) 2 +(A-L2) 2 +(A-L3) 2} / 3] 0.5 It is calculated as follows.

[0133] For example, the heating unit may be installed so that R2 in the following formula 2 falls within a predetermined range.

[0134] [Formula 2] R2=L C / n

[0135] In Equation 2, L C is the length of the catalyst section, and n is the number of heating units, where the length of the catalyst section may be in m.

[0136] The upper limit of R2 in Formula 2 may be about 10, 9, 7, 6, 5, 4, 3, 2, or 1, and the lower limit may be about 0.01, 0.05, 0.1, 0.2, 0.3, 0.4, 0.5, 0.6, 0.7, 0.8, or 0.9. R2 may be within a range that is greater than or equal to any one of the lower limits mentioned above; less than or equal to any one of the upper limits mentioned above; or greater than or equal to or exceeding any one of the lower limits mentioned above, but less than or equal to any one of the upper limits mentioned above.

[0137] The heating unit thus installed can be driven so that the absolute value of ΔT2 in the following equation 4 is within a predetermined range.

[0138] [Formula 4] △T2=(T HA -T CA ) / T CA ×100

[0139] T in Equation 4 HA is the average heating temperature of the heating unit, and T CA is the average temperature in the stabilization section.

[0140] The average heating temperature of the heating unit is the arithmetic mean of the heating temperatures of each heating unit, and the heating temperature of the heating unit may be the temperature of the heating unit set for heating or the temperature (core temperature) of the pipeline, internal passage, catalytic section, or non-catalytic section achieved by the heating unit.

[0141] The upper limit of the absolute value of ΔT2 in Equation 4 may be approximately 100%, 95%, 90%, 85%, 80%, 75%, 70%, 65%, 60%, 55%, 50%, 45%, 40%, 35%, 30%, 28%, or 26%, and the lower limit may be approximately 5%, 10%, 15%, 20%, 21%, 22%, 23%, 24%, or 25%. The absolute value of ΔT2 may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. ΔT2 may be a positive or negative number.

[0142] The heating unit may be present at one or more of the start point of the catalyst section, the middle point of the catalyst section, and the end point of the catalyst section, and may be present at all of these points, for example.

[0143] The term "start of catalyst section" refers to any point within the catalyst section that is within a certain distance from the point where the fluid first contacts the catalyst along the direction of fluid flow. For example, referring to FIG. 16, the start of the catalyst section is a distance L2 from the start of the catalyst region filled with catalyst 610, and R S The area at the start of the catalytic section is expressed as 100 × L / L C (L C is the length of the catalyst section) is 0% or more and 25% or less, 20% or less, 15% or less, 10% or less, 9% or less, or 8% or less.

[0144] The term "catalyst section end point" refers to any point within the catalyst section that is within a certain distance from the point where the fluid last contacts the catalyst along the direction of fluid flow. For example, referring to FIG. 16, the catalyst section end point is a distance L3 away from the end of the catalyst region filled with catalyst 610, and R E The area at the end of the catalytic section is expressed as 100 × L3 / LC (L C is the length of the catalyst section) is 0% or more and 25% or less, 20% or less, 15% or less, 10% or less, 9% or less, or 8% or less.

[0145] The term catalyst zone midpoint refers to any point within the catalyst zone that is not the beginning or end of said catalyst zone.

[0146] The heating unit may be located at the beginning of the catalyst section, at a midpoint of the catalyst section, and at an end of the catalyst section, and there may be one or more heating units at each location.

[0147] In such a case, in consideration of the desired effect, the heating units at each point can satisfy the following formula 13.

[0148] [Formula 13] T CS ≧T CM ≧T CE

[0149] T in Equation 13 CS is the average heating temperature of the heating unit located at the beginning of the catalyst section, and T CM is the average heating temperature of the heating unit located at the midpoint of the catalyst section, and T CE is the average heating temperature of the heating unit located at the end of the catalyst section.

[0150] In the above case, the heating unit can be driven so that the absolute value of ΔT3 in the following equation 14 and the absolute value of ΔT3 in the following equation 15 are within a predetermined range.

[0151] [Formula 14] △T3=(T CM -T CS ) / T CS ×100

[0152] [Formula 15] △T4=(T CE -T CM ) / T CM ×100

[0153] In Equations 14 and 15, T CS is the average heating temperature of the heating unit located at the beginning of the catalyst section, and T CM is the average heating temperature of the heating unit located at the midpoint of the catalyst section, and T CE is the average heating temperature of the heating unit located at the end of the catalyst section.

[0154] The lower limit of the absolute value of ΔT3 in Equation 14 may be approximately 1%, 5%, 10%, 15%, or 20%, and the upper limit may be approximately 150%, 140%, 130%, 120%, 110%, 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, or 25%. The absolute value of ΔT3 may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. ΔT3 may be a negative number.

[0155] The lower limit of the absolute value of ΔT4 in Equation 15 may be approximately 0.5%, 1%, 3%, 5%, or 7%, and the upper limit may be approximately 150%, 140%, 130%, 120%, 110%, 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, 25%, 20%, 15%, 10%, 9%, or 8%. The absolute value of ΔT4 may be greater than or exceeding any one of the lower limits; less than or equal to any one of the upper limits; or greater than or exceeding any one of the lower limits but less than or equal to any one of the upper limits. ΔT4 may be a negative number.

[0156] When two or more heating units are present at any one of the start point of the catalyst section, the middle point of the catalyst section, and the end point of the catalyst section, the heating temperature of the heating unit located at the start point of the catalyst section along the fluid flow direction may gradually increase, and the heating temperature of the heating units located at the middle point and the end point of the catalyst section may gradually decrease.

[0157] For example, when multiple heating units are present at the start of the catalyst section, the temperature change rate between the heating units may be a positive number, with an upper limit of 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, 15%, 10%, 8%, 6%, 4%, or 2%, and a lower limit of 0.5%, 1%, 3%, 5%, 7%, 9%, 11%, or 13%. The absolute value of the change rate may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. The rate of change of the heating temperature is calculated as 100×(H2-H1) / H1, where H1 is the temperature of the heating unit that forms the heating area that the fluid encounters first along the fluid flow direction, and H2 is the heating temperature of the heating unit that immediately follows the heating unit with heating temperature H1 along the fluid flow direction.

[0158] For example, when multiple heating units are present at the midpoint and / or end point of the catalyst section, the temperature change rate between the heating units may be a negative number, with the upper limit of its absolute value being approximately 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, 15%, 10%, 8%, 6%, 4%, or 2%, and the lower limit being approximately 0.5%, 1%, 3%, 5%, 7%, 9%, 11%, or 13%. The absolute value of the change rate may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. The rate of change of the heating temperature is calculated as 100×(H2-H1) / H1, where H1 is the temperature of the heating unit that forms the heating area that the fluid encounters first along the fluid flow direction, and H2 is the heating temperature of the heating unit that immediately follows the heating unit with heating temperature H1 along the fluid flow direction.

[0159] A heating unit may additionally be present at a point before the catalyst section.

[0160] The term "point before the catalyst section" refers to any point in the non-catalytic section before the fluid enters the catalyst section along the direction of fluid flow, and is within a certain distance from the point where the fluid first comes into contact with the catalyst along the direction of fluid flow. For example, referring to FIG. 16, the point before the catalyst section is a distance L1 from the start of the catalyst region filled with catalyst 610, and R B The area at the start of the catalytic section is expressed as 100 × L / L C (L C The lower limit of the value of 100×L / L (where L is the length of the catalytic section) can be 0%, 5%, or 10%, and the upper limit can be 25%, 20%, 15%, 10%, 9%, or 8%. C (L Cis the length of the catalytic section) may be in a range that is greater than or equal to any one of the aforementioned lower limits; less than or equal to any one of the aforementioned upper limits; or greater than or equal to or greater than any one of the aforementioned lower limits, but less than or equal to any one of the aforementioned upper limits.

[0161] In such a case, the heating unit may be configured to satisfy the following formula 16.

[0162] [Formula 16] T CS ≧T NS

[0163] T in Equation 16 CS is the average heating temperature of the heating unit located at the start of the catalyst section, and T NS is the average heating temperature of the heating unit at the point before the catalyst section.

[0164] In such a case, ΔT5 in the following formula 17 may be within a predetermined range.

[0165] [Formula 17] △T5=(T CS -T NS ) / T NS ×100

[0166] The lower limit of the absolute value of ΔT5 in Equation 17 may be approximately 1%, 5%, 10%, 15%, or 20%, and the upper limit may be approximately 150%, 140%, 130%, 120%, 110%, 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, or 25%. The absolute value of ΔT5 may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. ΔT5 may be a positive number.

[0167] For example, if there are multiple heating units before the catalyst section, the temperature change rate between the heating units may be a positive number, with an upper limit of 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, 15%, 10%, 8%, 6%, 4%, or 2%, and a lower limit of 0.5%, 1%, 3%, 5%, 7%, 9%, 11%, or 13%. The absolute value of the change rate may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. The rate of change of the heating temperature is calculated as 100×(H2-H1) / H1, where H1 is the temperature of the heating unit that forms the heating area that the fluid encounters first along the fluid flow direction, and H2 is the heating temperature of the heating unit that immediately follows the heating unit with heating temperature H1 along the fluid flow direction.

[0168] A heating unit may additionally be present at a point after the catalyst section.

[0169] The term "point after the catalyst section" refers to any point in the non-catalytic section after the fluid has passed through the catalyst section along the direction of fluid flow, and is within a certain distance from the point where the fluid last contacts the catalyst along the direction of fluid flow. For example, referring to FIG. 16, the point after the catalyst section is a distance L4 away from the end point of the catalyst section filled with catalyst 610, and R F The area at the start of the catalytic section is expressed as 100 × L / L C (L C is the length of the catalytic section) can be a region whose lower limit is 0%, 5%, 10%, 15%, 20%, or 25% and whose upper limit is 50%, 45%, 40%, 35%, 30%, 25%, 20%, 15%, 10%, 9%, or 8%. C (L Cis the length of the catalytic section) may be in a range that is greater than or equal to any one of the aforementioned lower limits; less than or equal to any one of the aforementioned upper limits; or greater than or equal to or greater than any one of the aforementioned lower limits, but less than or equal to any one of the aforementioned upper limits.

[0170] In the above case, the heating unit can be driven to satisfy the following equation 18:

[0171] [Formula 18] T CE ≧T NE

[0172] T in Equation 18 CE is the average heating temperature of the heating unit located at the end of the catalyst section, and T NE is the average heating unit heating temperature at the point after the catalyst section.

[0173] In such a case, ΔT6 in the following formula 19 may be within a predetermined range.

[0174] [Formula 19] △T6=(T NE -T CE ) / T CE ×100

[0175] T in Equation 18 CE is the average heating temperature of the heating unit located at the end of the catalyst section, and T NE is the average heating unit heating temperature at the point after the catalyst section.

[0176] The lower limit of the absolute value of ΔT6 in Equation 19 may be about 0.5%, 1%, 1.5%, or 2%, and the upper limit may be about 50%, 45%, 40%, 35%, 30%, 25%, 20%, 15%, 10%, 5%, 4%, 3%, or 2.5%. The absolute value of ΔT6 may be in a range that is equal to or greater than any one of the lower limits; equal to or less than any one of the upper limits; or equal to or greater than any one of the lower limits but equal to or less than any one of the upper limits. ΔT6 may be a negative number.

[0177] For example, if there are multiple heating units after the catalyst section, the temperature change rate between the heating units may be a negative number, with an upper limit of 100%, 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, 15%, 10%, 8%, 6%, 4%, 2%, or 1.5%, and a lower limit of 0.5%, 1%, 1.5%, or 2%. The absolute value of the change rate may be greater than or equal to any one of the lower limits; less than or equal to any one of the upper limits; or greater than or equal to any one of the lower limits but less than or equal to any one of the upper limits. The rate of change of the heating temperature is calculated as 100×(H2-H1) / H1, where H1 is the temperature of the heating unit that forms the heating area that the fluid encounters first along the fluid flow direction, and H2 is the heating temperature of the heating unit that immediately follows the heating unit with heating temperature H1 along the fluid flow direction.

[0178] By applying the above-mentioned reactor, the desired effect can be achieved.

[0179] The present specification also discloses a reaction method using the reactor.

[0180] The method is a method of carrying out a reaction using the above-described reactor, and may include transferring a fluid containing a reactant to an internal passage of a pipeline and independently transferring thermal energy to the internal passage using the plurality of heating units.

[0181] At this time, the details of the reaction device, the reaction target material, the fluid, etc. are the same as those described above.

[0182] Therefore, as described above, it may contain the carbon dioxide, be substantially free of water, and contain the organic hydrocarbon compounds described above.

[0183] In addition, as described above, during the reaction, the heating unit may be driven so that the catalyst section includes a stabilization section above a certain level. At this time, the specific details of the stabilization section, for example, the range of ΔT1 in Equation 3, the length L of the stabilization section, S The length L of the catalyst section C Ratio to L S / L C The range of T in the above formula 3 CA The scope of the above is as described above.

[0184] Furthermore, during the reaction, the reactor, pipeline, or heating unit satisfies the formula 5, and if necessary, T NCA T CL Ratio to T NCA / T CL can be driven so that the range of is the same as described above.

[0185] Furthermore, during the reaction, the reactor, pipeline, or heating unit satisfies the formula 6, and if necessary, T NCH T CH Ratio to T NCH / T CH can be driven so that the range of

[0186] Also, if necessary, the reactor, pipeline or heating unit can be driven so that the value of ΔR3 in Equation 7 can be in the range described above.

[0187] Also, if necessary, the reactor, pipeline or heating unit can be driven so that the value of ΔR4 in Equation 8 can be in the range described above.

[0188] Also, if necessary, the reactor, pipeline or heating unit can be driven so that the value of ΔR5 in Equation 9 can be in the range described above.

[0189] Also, if necessary, the reactor, pipeline or heating unit can be driven so that the value of ΔR6 in Equation 10 can be in the range described above.

[0190] Also, if necessary, the reactor, pipeline or heating unit can be driven so that the value of ΔR7 in Equation 11 can be in the range described above.

[0191] In addition, the heating units in the reaction apparatus may be installed so that the value of R1 in Equation 1 is within the above-mentioned range, and in this case, the standard deviation of the interval between the heating units may also be within the above-mentioned range.

[0192] In addition, the heating unit in the reaction apparatus may be installed so that the value of R2 in the formula 2 falls within the above-mentioned range.

[0193] In addition, the heating unit in the reaction apparatus may be driven so that the value of ΔT2 in Equation 4 falls within the aforementioned range.

[0194] Furthermore, the heating unit in the reaction apparatus can be driven to satisfy the formula (13), and if necessary, can be driven so that the value of ΔT3 in the formula (14) and / or ΔT4 in the formula (15) falls within the aforementioned range.

[0195] When two or more heating units are present at any one of the start point of the catalyst section, the middle point of the catalyst section, and / or the end point of the catalyst section, the heating units may be driven so that the temperature change rate is within the above-mentioned range depending on the point.

[0196] In addition, the heating unit in the reaction apparatus can be driven to satisfy the formula (16), and if necessary, can be driven so that the value of ΔT5 in the formula (17) falls within the above-mentioned range.

[0197] When two or more heating units are present at a point before the catalyst section, the heating units may be driven at different points so that the temperature change rate falls within the above-mentioned range.

[0198] In addition, the heating unit in the reaction apparatus can be driven to satisfy the formula (18), and if necessary, can be driven so that the value of ΔT6 in the formula (19) falls within the above-mentioned range.

[0199] When two or more heating units are present at a point after the catalyst section, the heating units may be driven at different points so that the temperature change rate falls within the above-mentioned range.

[0200] This specification also discloses a synthesis gas production apparatus. This synthesis gas production apparatus can be the above-described reactor or can include the reactor. The target synthesis gas can be produced by carrying out a steam methane reforming (SMR) process or a dry methane reforming (DRM) process in the reactor. This reactor or synthesis gas production apparatus can be a device in which the DRM process is carried out, i.e., a DRM device, or a part thereof. [Effects of the Invention]

[0201] This specification discloses a reactor, a reaction method using the reactor, and uses of the reactor. The reactor can solve the coking problem that can occur during the synthesis gas production process without applying a costly and energy-intensive method of introducing excessive amounts of steam or carbon dioxide. The reactor can also achieve the above objectives in a DRM process that does not use steam. This specification also discloses a reaction method using the reactor and uses of the reactor. [Brief explanation of the drawings]

[0202] [Figure 1] 1 is a diagram of an exemplary reactor. [Figure 2] 1 is a diagram illustrating an exemplary pipeline configuration. [Figure 3] 1 is a drawing showing a cross-sectional configuration of an exemplary pipeline. [Figure 4] 1 is a diagram of a pipeline for explaining a heating region. [Figure 5] 1 is an illustration of a reactor including a catalyst section. [Figure 6] 1 is an illustration of a reactor including a catalyst section. [Figure 7] 1 is a diagram of a pipeline to explain the core temperature. [Figure 8] 1 is a drawing of a pipeline illustrating a catalyst section. [Figure 9] 10 is a diagram illustrating an embodiment of an external heat source. [Figure 10] 1 shows the temperature relative to the external heat source in Example 1. [Figure 11] 1 is a graph showing the temperature depending on the fluid flow direction in the pipeline of Example 1. [Figure 12] 1 shows the temperature relative to the external heat source in Comparative Example 1. [Figure 13] 10 is a graph showing the temperature according to the fluid flow direction in the pipeline of Comparative Example 1. [Figure 14] 10 shows the temperature relative to the external heat source in Comparative Example 2. [Figure 15]10 is a graph showing the temperature depending on the fluid flow direction in the pipeline of Comparative Example 2. [Figure 16] 1 is a diagram illustrating a point before a catalyst section, a start point, a middle point, and an end point of the catalyst section, and a point after the catalyst section. DETAILED DESCRIPTION OF THE INVENTION

[0203] Hereinafter, the reactors and the like disclosed in the present specification will be described in more detail through examples and comparative examples, but the scope of the reactors and the like is not limited to the contents presented below.

[0204] Example 1

[0205] The following reaction apparatus was implemented to obtain the results.

[0206] The pipeline 100 has a total length (L) of about 12 m and a circular cross section (the shape shown on the left side of Figure 3). X ) from a point that is about 2.4 m away from the point (P X A fixed bed of DRM (Dry Reforming of Methane) catalyst was continuously filled from the pipeline 100 to a point about 10 m away to form a catalyst section. Nickel-doped perovskite metal oxide was used as the catalyst, and the catalyst was uniformly filled throughout the catalyst section. The internal passage of the pipeline 100 that was not charged with the catalyst was the non-catalyst section.

[0207] The point P of the pipeline 100 x An external heat source 400 was installed in a form surrounding the pipeline 100 (form of FIG. 9) at a point (heat source order: 1) about 1.5 m away from the point P. An electric indirect heating unit 400 was used as the external heat source. xThe external heat source 400 was installed so that heating regions 130 were formed about 0.2 m (P) on both sides of the center, which was about 1.5 m from the center. The average separation distance (d) between the external heat source 400 and the surface 110 of the pipeline 100 was about 1 m. The external heat source 400 was installed so that nine sub-heat sources 430 were provided in the circumferential direction of the pipeline 100. Figure 9 shows a simplified diagram of the installation method of the external heat source 400.

[0208] The point P of the pipeline 100 x External heat sources 400 were installed in the same manner at points about 3 m away (heat source order: 2), 4.5 m away (heat source order: 3), 6 m away (heat source order: 4), 7.5 m away (heat source order: 5), 9 m away (heat source order: 6), 10.5 m away (heat source order: 7), and 12 m away (heat source order: 8) from the pipeline 100. Each external heat source 400 was installed so as to be able to transfer thermal energy to the pipeline 100 independently.

[0209] The heating temperatures of the eight external heat sources 400 were controlled in the manner shown in Fig. 10. Fig. 10 shows the temperature of the center portion of the internal passage of the pipeline achieved by each external heat source 400 in Example 1 on the y-axis, in units of Celsius (°C). The x-axis shows the temperature of the point P x The coordinate of the point P is set to 0 and the distance (unit: m) from it is displayed, and the numbers indicate each external heat source. Therefore, the external heat source 400 installed at a point about 1.5 m on the x-axis is displayed as 1, and then the point P x The external heat sources 400 installed at points about 3 m, 4.5 m, 6 m, 7.5 m, 9 m, 10.5 m, and 12 m away from the target are indicated by 2, 3, 4, 5, 6, 7, and 8, respectively.

[0210] As shown in Figure 10, the second external heat source 400 transfers the most heat energy, and the area corresponding to this part in the pipeline 100 corresponds to the reaction start section of the catalytic section (or the starting point of the catalytic section).

[0211] In a state where the pipeline 100 is stabilized to have the distribution of the central temperature as shown in FIG. 10, a reaction target material, which is a mixture of methane (CH4) and carbon dioxide (CO2) in a ratio of 1:1.12 (CH4:CO2), is fed to the point P of the pipeline 100 at a rate of 0.07 kg / s. x was allowed to flow into

[0212] The pipeline 100 was installed vertically at a 90-degree angle from the ground, and the fluid flowed into the pipeline 100 under the influence of gravity. The fluid did not contain steam, and the reaction was generally maintained within a range of approximately 3 barg to 6 barg.

[0213] The DRM reaction was carried out on the fluid under the temperature distribution shown in Figure 10. As a result, under the above conditions, the conversion rate of methane (CH4) was about 80% in the steady-state of the reaction.

[0214] FIG. 11 shows the flow direction D of the fluid in the pipeline 100 during the reaction in Example 1. F 11 is a graph showing the center temperature measured at various points along the catalyst section 600. Referring to FIG. 11, it can be seen that a stabilization section was formed from the point approximately 50% of the length of the catalyst section 600 after the start of the catalyst section 600 to the point where the catalyst section 600 ends. The average center temperature (T CA ) was about 850°C. S / T CA x100, T CA is the average central temperature of the stabilization section, and T S is the temperature T at any point within the stabilization section i and the aforementioned T CAThe absolute value of the difference between the average and minimum temperatures was confirmed to be less than 0.2%. The average central temperature of the non-catalytic section was approximately 836.7°C, the minimum central temperature of the catalytic section was approximately 800°C, the maximum central temperature of the non-catalytic section was approximately 900°C, the maximum central temperature of the catalytic section was approximately 855°C, and the minimum central temperature of the non-catalytic section was approximately 770°C.

[0215] Comparative Example 1

[0216] An existing, general roof burner was implemented. To implement the same thermal energy supply distribution as when the roof burner (assuming a non-premixed flame length of 3 m) is applied in a state similar to Example 1, an external heat source 400 was installed to control the thermal energy, as shown in Figure 12. Referring to Figure 12, it is shown that external heat source 400 No. 3 transfers the most thermal energy, and the corresponding area in the pipeline 100 corresponds to the reaction continuation section of the catalytic section. Figure 13 shows a graph of the central temperature measured at each point along the fluid flow direction DF of the pipeline 100 for Comparative Example 1. Referring to Figure 13, the average central temperature (T CA ) was approximately 785°C. In addition, ΔT1 in Equation 3 exceeded 2% at a specific point in the section from the 50% point of the catalyst section 600 to the end point of the catalyst section 600. In addition, the average temperature in the non-catalytic section was approximately 773.3°C, the minimum temperature in the catalyst section was approximately 730°C, the maximum temperature in the non-catalytic section was approximately 830°C, and the maximum temperature in the catalyst section was approximately 970°C.

[0217] Comparative Example 2

[0218] Although the present invention is the same as that of Example 1, the external heat source 400 was controlled as shown in FIG. 14 to supply a constant amount of heat energy. FIG. 15 shows a graph of the center temperature measured at each point along the fluid flow direction DF of the pipeline 100 for Comparative Example 2. Referring to FIG. 15, the average center temperature (T CA ) was approximately 875°C. In addition, ΔT1 in Equation 3 exceeded 2% at a specific point in the section from the 50% point of the catalyst section 600 to the end point of the catalyst section 600. In addition, the average temperature in the non-catalytic section was approximately 856.7°C, the minimum temperature in the catalyst section was approximately 740°C, the maximum temperature in the non-catalytic section was approximately 880°C, and the maximum temperature in the catalyst section was approximately 973°C.

Claims

1. a pipeline having an internal passageway formed therein through which a fluid can flow; a catalytic section present in the internal passage; and a plurality of heating units; The reaction apparatus, wherein the plurality of heating units are installed so as to be able to independently transfer heat energy to the internal passage.

2. 10. The reactor of claim 1, wherein the catalyst section comprises an endothermic catalyst.

3. Length of catalyst section L Ｃ The length of the pipeline L Ｐ Ratio L to Ｃ / L Ｐ 2. The reactor of claim 1, wherein is 0.3 or more.

4. 10. The reactor of claim 1, wherein the catalyst section is a continuous catalyst section.

5. 10. The reactor of claim 1, wherein the plurality of heating units comprises electrical heating units.

6. 6. The reactor of claim 5, wherein the electrical heating unit is a direct electrical heating unit, an indirect electrical heating unit or an induction heating unit.

7. R in the following formula 1 １ The reaction apparatus according to claim 1, wherein the heating unit is installed so that [Formula 1] R １ =L Ｃ / H Ｉ In Equation 1, L Ｃ is the length of the catalyst section, and H Ｉ is the average spacing between heating units.

8. R in the following formula 2 ２ The reaction apparatus according to claim 1, wherein the heating unit is installed so that [Formula 2] R ２ =L Ｃ / n In Equation 2, L Ｃ is the length of the catalyst section and n is the number of heating units.

9. The heating unit is configured such that the catalyst section is １ The reactor of claim 1, wherein the reactor is configured to include a stabilization section in which the [Formula 3] △T １ =T Ｓ / T ＣＡ ×100 In Equation 3, T ＣＡ is the average temperature in the stabilization section, and T Ｓ is the temperature T at any point within the stabilization section ｉ and the aforementioned T ＣＡ is the absolute value of the difference between

10. Length of stabilization section L Ｓ The length of the catalyst section L Ｃ Ratio L to Ｓ / L Ｃ The reaction apparatus according to claim 9, wherein the heating unit is installed so that the value of the temperature is 0.2 or more.

11. T ＣＡ 10. The reactor of claim 9, wherein the temperature is in the range of 750°C to 1,000°C.

12. ΔT in the following formula 4 ２ The reaction apparatus according to claim 9, wherein the heating unit is installed so that the absolute value of is in the range of 5% to 60%: [Formula 4] △T ２ =(T ＨＡ -T ＣＡ ) / T ＣＡ ×100 In Equation 4, T ＨＡ is the average heating temperature of the heating unit, and T ＣＡ is the average temperature in the stabilization section.

13. 2. The reactor of claim 1, wherein the pipeline additionally comprises a non-catalytic section, and the heating unit is installed so that the following formula 5 is satisfied: [Formula 5] T ＮＣＡ ≧T ＣＬ In Equation 5, T ＮＣＡ is the average temperature of the non-catalytic section, and T ＣＬ is the minimum temperature in the catalyst section.

14. 10. The reactor of claim 1, wherein the pipeline additionally comprises a non-catalytic section, and the heating unit is installed so that the following formula 6 is satisfied: [Formula 6] T ＮＣＨ ≧T ＣＨ In Equation 6, T ＮＣＨ is the maximum temperature of the non-catalytic section, and T ＣＨ is the maximum temperature in the catalyst section.

15. The pipeline additionally includes a non-catalytic section, and the ΔR ３ The reactor of claim 9, wherein the absolute value of is 20% or less: [Formula 7] △R ３ =(T ＮＣＡ -T ＣＡ ) / T ＣＡ ×100 In Equation 7, T ＣＡ is the average temperature in the stabilization section, and T ＮＣＡ is the average temperature of the non-catalytic section.

16. ΔR in the following formula 8 ４ and the absolute value of ΔR in the following equation 9 ５ The reactor of claim 9, wherein the absolute values ​​of [Formula 8] △R ４ =(T ＣＨ -T ＣＡ ) / T ＣＡ ×100 [Formula 9] △R ５ =(T ＣＬ -T ＣＡ ) / T ＣＡ ×100 In Equations 8 and 9, T ＣＡ is the average temperature in the stabilization section, and T ＣＨ is the maximum temperature in the catalyst section, and T ＣＬ is the minimum temperature in the catalyst section.

17. The pipeline includes an additional non-catalytic section. ６ and the absolute value of ΔR in the following equation 11 ７ The reactor of claim 9, wherein the absolute values ​​of [Formula 10] △R ６ =(T ＮＣＨ -T ＣＡ ) / T ＣＡ ×100 [Formula 11] △R ７ =(T ＣＬ -T ＣＡ ) / T ＣＡ ×100 In Equations 10 and 11, T ＣＡ is the average temperature in the stabilization section, and T ＮＣＨ is the maximum temperature in the non-catalytic section, and T ＨＣＬ is the minimum temperature in the non-catalytic section.

18. The heating units are located at the beginning of the catalyst section, the middle of the catalyst section, and the end of the catalyst section, respectively; The following formula 12 is satisfied, and ΔT in the following formula 13 is satisfied. ３ is a negative number whose absolute value is in the range of 1% to 150%, ΔT in the following formula 14 ４ is a negative number, and its absolute value is within a range of 0.5% to 150%; [Formula 12] T ＣＳ ≧T ＣＭ ≧T ＣＥ [Formula 13] △T ３ =(T ＣＭ -T ＣＳ ) / T ＣＳ ×100 [Formula 14] △T ４ =(T ＣＥ -T ＣＭ ) / T ＣＭ ×100 In equations 12 to 14, T ＣＳ is the average heating temperature of the heating unit located at the start of the catalyst section, and T ＣＭ is the average heating temperature of the heating unit located at the midpoint of the catalyst section, and T ＣＥ is the average heating temperature of the heating unit located at the end of the catalyst section.

19. A heating unit is additionally included at a point before the catalyst section, and the following equation 15 is satisfied, and the ΔT of the following equation 16 is ５ is a positive number, and its absolute value is within the range of 1% to 150%. [Formula 15] T ＣＳ ≧T ＮＳ [Formula 16] △T ５ =(T ＣＳ -T ＮＳ ) / T ＮＳ ×100 In Equations 15 and 16, T ＣＳ is the average heating temperature of the heating unit located at the start of the catalyst section, and T ＮＳ is the average heating temperature of the heating unit at the point before the catalyst section.

20. A heating unit is added at a point after the catalyst section, and the following equation (17) is satisfied. ６ is a negative number, and its absolute value is within the range of 0.5% to 50%. [Formula 17] T ＣＥ ≧T ＮＥ [Formula 18] △T6=(T ＮＥ -T ＣＥ ) / T ＣＥ ×100 In Equations 17 and 18, T ＣＥ is the average heating temperature of the heating unit located at the end of the catalyst section, and T ＮＥ is the average heating temperature of the heating unit at the point after the catalyst section.

21. 10. A method of carrying out a reaction using the reactor of claim 1, comprising: While moving a fluid containing a substance to be reacted through the internal passage of the pipeline, The method includes using two or more heating units to independently transfer heat energy to the interior passageway.

22. 22. The method of claim 21, wherein the fluid comprises carbon dioxide, is free of water, and comprises an organic hydrocarbon compound.

23. The heating unit is configured such that the catalyst section is T １ 22. The method of claim 21, wherein thermal energy is transferred to the internal passageway to include a stabilization section where the thermal energy transfer coefficient is 2% or less. [Formula 3] △T １ =T Ｓ / T ＣＡ ×100 In Equation 3, T ＣＡ is the average temperature in the stabilization section, and T Ｓ is the temperature T at any point within the stabilization section ｉ and the aforementioned T ＣＡ is the absolute value of the difference between

24. Length of stabilization section L Ｓ The length of the catalyst section L Ｃ Ratio L to Ｓ / L Ｃ 24. The method of claim 23, wherein is greater than or equal to 0.

2.

25. T ＣＡ 24. The method of claim 23, wherein the temperature is in the range of 750°C to 1,000°C.

26. The heating unit is calculated by the following formula 4: ２ 24. The method of claim 23, wherein thermal energy is transferred to the internal passage so that the absolute value of [Formula 4] △T ２ =(T ＨＡ -T ＣＡ ) / T ＣＡ ×100 In Equation 4, T ＨＡ is the average heating temperature of the heating unit, and T ＣＡ is the average temperature in the stabilization section.

27. 22. The method of claim 21, wherein the pipeline additionally includes a non-catalytic section, and the heating unit transfers thermal energy to the interior passage such that the following equation 5 is satisfied: [Formula 5] T ＮＣＡ ≧T ＣＬ In Equation 5, T ＮＣＡ is the average temperature of the non-catalytic section, and T ＣＬ is the minimum temperature in the catalyst section.

28. 22. The method of claim 21, wherein the pipeline additionally includes a non-catalytic section, and the heating unit transfers thermal energy to the interior passage so that the following equation (6) is satisfied: [Formula 6] T ＮＣＨ ≧T ＣＨ In Equation 6, T ＮＣＨ is the maximum temperature of the non-catalytic section, and T ＣＨ is the maximum temperature in the catalyst section.

29. The pipeline additionally includes a non-catalytic section, and the heating unit is ３ 24. The method of claim 23, wherein thermal energy is transferred to the internal passage so that the absolute value of [Formula 7] △R ３ =(T ＮＣＡ -T ＣＡ ) / T ＣＡ ×100 In Equation 7, T ＣＡ is the average temperature in the stabilization section, and T ＮＣＡ is the average temperature of the non-catalytic section.

30. ΔR in the following formula 8 ４ and the absolute value of ΔR in the following equation 9 ５ 24. The method of claim 23, wherein the heating unit transfers thermal energy to the internal passage so that the absolute values ​​of [Formula 8] △R ４ =(T ＣＨ -T ＣＡ ) / T ＣＡ ×100 [Formula 9] △R ５ =(T ＣＬ -T ＣＡ ) / T ＣＡ ×100 In Equations 8 and 9, T ＣＡ is the average temperature in the stabilization section, and T ＣＨ is the maximum temperature in the catalyst section, and T ＣＬ is the minimum temperature in the catalyst section.

31. The pipeline additionally includes a non-catalytic section, and ΔR in Eq. ６ and the absolute value of ΔR in the following equation 11 ７ 24. The method of claim 23, wherein the heating unit transfers thermal energy to the internal passage so that the absolute values ​​of [Formula 10] △R ６ =(T ＮＣＨ -T ＣＡ ) / T ＣＡ ×100 [Formula 11] △R ７ =(T ＣＬ -T ＣＡ ) / T ＣＡ ×100 In Equations 10 and 11, T ＣＡ is the average temperature in the stabilization section, and T ＮＣＨ is the maximum temperature in the non-catalytic section, and T ＨＣＬ is the minimum temperature in the non-catalytic section.

32. The heating units are located at the beginning of the catalyst section, the middle of the catalyst section, and the end of the catalyst section, respectively; The following formula 12 is satisfied: ΔT in the following formula 13 ３ is a negative number whose absolute value is in the range of 1% to 150%, ΔT in the following formula 14 ４ 22. The method of claim 21, wherein the heating unit transfers thermal energy to the internal passageway such that is a negative number whose absolute value is in the range of 0.5% to 150%. [Formula 12] T ＣＳ ≧T ＣＭ ≧T ＣＥ [Formula 13] △T ３ =(T ＣＭ -T ＣＳ ) / T ＣＳ ×100 [Formula 14] △T ４ =(T ＣＥ -T ＣＭ ) / T ＣＭ ×100 In equations 12 to 14, T ＣＳ is the average heating temperature of the heating unit located at the start of the catalyst section, and T ＣＭ is the average heating temperature of the heating unit located at the midpoint of the catalyst section, and T ＣＥ is the average heating temperature of the heating unit located at the end of the catalyst section.

33. A heating unit is additionally included at a point before the catalyst section, and the following equation 15 is satisfied, and the ΔT of the following equation 16 is ５ is a positive number, and the heating unit transfers thermal energy to the internal passage so that its absolute value is within a range of 1% to 150%. [Formula 15] T ＣＳ ≧T ＮＳ [Formula 16] △T ５ =(T ＣＳ -T ＮＳ ) / T ＮＳ ×100 In Equations 15 and 16, T ＣＳ is the average heating temperature of the heating unit located at the start of the catalyst section, and T ＮＳ is the average heating temperature of the heating unit at the point before the catalyst section.

34. A heating unit is added at a point after the catalyst section, and the following equation (17) is satisfied. ６ is a negative number, and the heating unit transfers thermal energy to the internal passage so that its absolute value is within a range of 0.5% to 50%. [Formula 17] T ＣＥ ≧T ＮＥ [Formula 18] △T6=(T ＮＥ -T ＣＥ ) / T ＣＥ ×100 In Equations 17 and 18, T ＣＥ is the average heating temperature of the heating unit located at the end of the catalyst section, and T ＮＥ is the average heating temperature of the heating unit at the point after the catalyst section.

35. A synthesis gas production system comprising the reactor of claim 1.

36. A DRM device comprising the reaction device of claim 1.

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