Fixed bed catalytic reactor regeneration method and apparatus

Abstract

The invention relates to a method and a device for regenerating a fixed bed catalytic reactor, in particular to a method and a device for regenerating a catalyst in a process for producing acrylic acid from lactic acid.

Description

TECHNICAL FIELD

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS

[0002] This application claims priority to and the benefit of Korean Patent Application No. 10-2023-0176551, filed on December 7, 2023, and Korean Patent Application No. 10-2024-0176683, filed on December 2, 2024, the disclosures of which are incorporated by reference herein in their entireties.

[0003] The present invention relates to a regeneration method and apparatus of a fixed bed catalytic reactor, and more particularly, to a regeneration method and apparatus of a catalyst in a process of producing acrylic acid from lactic acid. BACKGROUND

[0004] Acrylic acid is an organic compound having both a carboxylic acid and an unsaturated double bond in its molecule, and is used in various industrial fields since it has a very simple structure and can be polymerized and simultaneously converted into various materials.

[0005] Specifically, acrylic acid can be used as polyacrylic acid required for producing superabsorbent polymers, adhesive adhesives, paints, etc., or can be used as a raw material for producing other types of acrylate monomers, or can also be used as a raw material for polymerization with various other monomers such as acrylamide, acrylonitrile, styrene, alpha-olefin, etc.

[0006] The acrylic acid is generally produced by using propylene produced in a refining and separation process of crude oil, such as naphtha cracking.

[0007] However, recently, as concerns about depletion of crude oil and environmental problems are increasing, interest in a method of producing acrylic acid using an environmentally friendly raw material is increasing. SUMMARY

[0008] [TECHNICAL PROBLEM]

[0009] An object of the present disclosure is to provide a method and apparatus for regenerating a fixed bed catalytic reactor, which can stably regenerate a catalyst while reducing catalyst regeneration costs.

[0010] [TECHNICAL SOLUTION]

[0011] To achieve the above object, according to the present disclosure, there is provided a method for regenerating a fixed bed catalytic reactor, the method including the steps of: supplying a feed containing lactic acid gas into a first reactor filled with a catalyst to perform a lactic acid dehydration reaction; separating acrylic acid and a by-product from a reaction product; adding the by-product to a regenerative thermal oxidizer (RTO); and adding a gas discharged from the regenerative thermal oxidizer to a second reactor filled with a catalyst to regenerate the catalyst.

[0012] According to one embodiment, the reaction product can contain 5-30 wt% of acrylic acid and 1-15 wt% of by-products other than water.

[0013] According to one embodiment, the by-products added to the regenerative thermal oxidizer can include at least one selected from the group consisting of acetaldehyde, 2-pentanedione, lactic acid, carbon dioxide, and carbon monoxide.

[0014] According to one embodiment, the regenerative thermal oxidizer can be operated at a temperature condition of 300 to 900℃.

[0015] According to one embodiment, the gas discharged from the regenerative thermal oxidizer can contain 0.5 to 10 vol% of oxygen.

[0016] According to one embodiment, the regeneration method can further include a step of controlling the temperature of the gas discharged from the regenerative thermal oxidizer to 100-500℃.

[0017] According to one embodiment, the second reactor can be operated at 300 to 500℃.

[0018] Further, according to the present disclosure, there is provided an apparatus for regenerating a fixed bed catalytic reactor, the apparatus including: a first reactor of a fixed bed isothermal type filled with a catalyst; a separator that separates the product of the first reactor; a regenerative thermal oxidizer that burns by-products discharged from the upper portion of the separator; and a second reactor of a fixed bed isothermal type filled with a catalyst and supplied with gas discharged from the regenerative thermal oxidizer.

[0019] According to one embodiment, the regeneration apparatus can further include a heat exchanger that cools the gas discharged from the regenerative thermal oxidizer and supplies it to the second reactor. The heat exchanger can be a steam generator.

[0020] As used herein, the terms "first", "second", and the like are used herein to explain various constituent elements, and the terms are used only to distinguish one constituent element from another.

[0021] Further, the technical terms used herein are used only to explain the exemplary embodiments, and are not intended to limit the scope of the present disclosure.

[0022] The singular forms "a," "an," and "the" are intended to include the plural forms as well, unless the context clearly indicates otherwise.

[0023] It should be understood that the terms "comprise", "include", "have", and the like are used herein to designate the presence of the stated features, numbers, steps, components, or combinations thereof, but do not preclude the presence or addition of one or more other features, numbers, steps, components, or combinations thereof.

[0024] Further, as used herein, where a layer or element is referred to as being formed "on" or "over" another layer or element, it is meant that the layer or element is directly formed on the layer or element, or that other layers or elements can additionally be formed therebetween, on the subject, or on the substrate.

[0025] Although the present disclosure can have various forms and can be variously modified, specific examples will be exemplified and explained in detail below. However, it is not intended to limit the present disclosure to the specific disclosure, and it should be understood that the present disclosure includes all modifications, equivalents, or alternatives thereof without departing from the spirit and technical scope of the present disclosure.

[0026] Hereinafter, the present disclosure is discussed in detail.

[0027] According to one aspect of the present disclosure, there is provided a method for regenerating a fixed bed catalytic reactor, the method including the steps of: supplying a feed containing lactic acid gas to a first reactor filled with a catalyst to perform a lactic acid dehydration reaction; separating acrylic acid and by-products from a reaction product; adding the by-products to a regenerative thermal oxidizer (RTO); and adding a gas discharged from the regenerative thermal oxidizer to a second reactor filled with a catalyst to regenerate the catalyst.

[0028] A process of producing acrylic acid by gas phase dehydration of lactic acid is mainly performed under an acid catalyst. At this time, lactic acid is contained as a reactant, acrylic acid is contained as a product, and an olefin compound is contained as an intermediate product during the reaction, and thus coke is often formed on the surface of the catalyst. The coke formed on the surface of the catalyst can block active sites of the catalyst and cause deactivation of the catalyst. In addition, a pressure difference before and after the catalyst layer rapidly increases due to the accumulated coke, which can interrupt the process. As a result, excessive coke deposited on the catalyst layer inhibits the yield of acrylic acid as a target product.

[0029] Therefore, the catalyst used in the method of producing acrylic acid by the gas phase dehydration reaction of lactic acid requires a process for removing coke formed on the catalyst layer through a regeneration process. Coke is a carbon deposit, and in order to remove the coke, the reactor operation is usually stopped and oxygen-containing air is injected to burn and remove the coke. At this time, the combustion reaction of the coke is an exothermic reaction, and hot spots are formed on the catalyst, so that a sintering phenomenon of the catalyst can occur in a high-temperature regeneration process.

[0030] Therefore, in the process of producing acrylic acid by the gas phase dehydration reaction of lactic acid, it is important to control the hot spot temperature of the catalyst during the catalyst regeneration process. An inert gas is usually used together with oxygen to control the hot spot temperature during the catalyst regeneration and to reduce the oxygen partial pressure. If nitrogen, which is mainly used as an inert gas, is added alone during the regeneration, this becomes a cause of increasing the process cost.

[0031] Accordingly, the present inventors found that, in order to reduce the cost of the regeneration process, the gas discharged from the regeneration-type thermal oxidizer for treating the post-acrylic acid production by-product is used as a high-temperature inert gas, thereby enabling reduction of the process cost, completing the present application.

[0032] First, the method for producing a feed containing a lactic acid gas, which is a reaction product of the present disclosure, is not particularly limited, and the feed can be produced by a conventional method in the art, but the method described below can be used as an example.

[0033] The lactic acid gas can be produced by evaporating a lactic acid aqueous solution. The lactic acid aqueous solution can preferably have a concentration range of about 10 wt% to about 80 wt%.

[0034] If the concentration of lactic acid is too low, the efficiency of the evaporation step and the efficiency of the dehydration reaction of the first step become too low, and if the concentration of lactic acid is too high, the content of oligomers or the like in the aqueous solution becomes high, which can cause a problem of promoting the production of by-products, reducing the efficiency of the dehydration reaction.

[0035] Further, the evaporation reaction of lactic acid can be performed under temperature conditions of about 200°C to 300°C. If the temperature of the evaporation reaction is too low, the evaporation efficiency is reduced, and if the temperature of the evaporation reaction is too high, decarboxylation or decarbonylation of the evaporated lactic acid molecules can mainly occur, which can cause a problem of promoting the production of aldehydes.

[0036] Then, the feed containing the lactic acid gas can be supplied to a reactor filled with a catalyst to perform a lactic acid dehydration reaction.

[0037] The feed containing the lactic acid gas can be continuously supplied to a catalyst portion in which the catalyst is present according to the flow of a carrier gas. The carrier gas can be an inert gas, and nitrogen or the like can be used.

[0038] Further, the reaction can be performed under temperature conditions of about 300°C to about 400°C. If the reaction temperature is too low, the lactic acid conversion rate and the acrylic acid yield are reduced, and if the reaction temperature is too high, there can be a problem of an increase in the amount of by-products formed.

[0039] Further, the catalyst can include at least one of a calcium phosphate-based catalyst, a sodium phosphate-based catalyst, and an aluminum phosphate-based catalyst, and other reaction conditions can be used without particular limitation as long as they are generally used in the technical field to which the present application pertains, unless contrary to the definitions herein. As an example, the catalyst can include CaSO4 / Na2SO4; Na4P2O7 / CaSO4; Na4P2O7 / Ca3(PO4)2; NaH2PO4-NaHCO3 / SiO2; AlPO4-NH3; Ca3(PO4)2 / CaSO4; Ca2P2O7; Ca5(PO4)3(OH), etc.

[0040] Further, according to one embodiment, the production method can be batch type or continuous type, but it is preferably continuous type equipped with a catalyst layer, in which the reaction is continuously transferred into the reactor with lactic acid gas, and also the acrylic acid is continuously obtained as a dehydration reaction product.

[0041] According to one embodiment, the reaction product can contain 5-30 wt% of acrylic acid and 1-15 wt% of by-products other than water. Preferably, the reaction product can contain 8-28 wt%, or 10-25 wt% of acrylic acid, and 3-12 wt%, or 5-10 wt% of by-products other than water.

[0042] In the course of the lactic acid dehydration reaction, by-products can be produced along with the acrylic acid due to side reactions. The by-products can include water, acetaldehyde, carbon monoxide, carbon dioxide, dilution gas, low-boiling by-products, and high-boiling by-products, in addition to the acrylic acid, and can also include unreacted lactic acid. Therefore, a step of separating the target product, i.e., the acrylic acid and the by-products, from the reaction product formed after the above lactic acid dehydration reaction step needs to be performed.

[0043] The step of separating the acrylic acid and the by-products can be performed by applying methods commonly used in the art. As an example, the reaction product stream can be supplied to a cooling tower to be condensed, and then the discharge stream containing the acrylic acid can be supplied to a distillation tower to separate the acrylic acid and the by-products by distillation, or the reaction product can be condensed in a plurality of cooling towers, and then the acrylic acid and the by-products can be separated from each other using an extractant in an extraction tower.

[0044] Further, in the above process, if necessary, devices such as heat exchangers, valves, pumps, separators, mixers, etc. can also be included.

[0045] The present disclosure includes a step of adding the by-products separated from the reaction product containing the acrylic acid to a regenerative thermal oxidizer (RTO). In general, the regenerative thermal oxidizer refers to a device that stores waste heat by directly contacting exhaust gas, reuses the stored heat, incinerates, and removes volatile organic compound gas generated in the process. The regenerative thermal oxidizer can include a combustion chamber and a predetermined number of beds made of a heat storage agent to increase the heat recovery rate.

[0046] According to one embodiment, the by-products added to the regenerative thermal oxidizer can include at least one selected from the group consisting of acetaldehyde, 2-pentanedione, lactic acid, carbon dioxide, carbon monoxide, etc.

[0047] According to one embodiment, the regenerative thermal oxidizer can be operated at a temperature condition of 300 to 900℃. If the temperature is less than 300℃, complete combustion can not be achieved, and if the temperature is greater than 900℃, there can be a problem of thermal damage to the regenerative thermal oxidizer in the regenerative thermal oxidizer. Preferably, the regenerative thermal oxidizer can be operated at a temperature condition of 300 to 900℃, 400 to 850℃, or 500 to 800℃. Meanwhile, the regenerative thermal oxidizer operates at a temperature within the above range, so that the temperature of the gas discharged from the regenerative thermal oxidizer can be adjusted to the above range.

[0048] Further, according to one embodiment, the gas discharged from the regenerative thermal oxidizer can include 0.5 to 10% by volume of oxygen. The inclusion of oxygen within the above range can provide an oxygen partial pressure suitable for catalyst regeneration in the second reactor described below, so that the hot spot of the catalyst can be adjusted to an appropriate temperature during the coke combustion process. Preferably, the gas can include 0.5 to 10% by volume, 1 to 8% by volume, or 2 to 5% by volume of oxygen.

[0049] Further, the gas discharged from the regenerative thermal oxidizer can include nitrogen, carbon dioxide, carbon monoxide, water, etc. in addition to oxygen.

[0050] According to one embodiment, a step of adjusting the temperature of the gas discharged from the regenerative thermal oxidizer to 100 to 500℃ can also be included. As an example, this step can be performed by a method including adding the gas discharged from the regenerative thermal oxidizer to a steam generator to generate steam by heat exchange, and adjusting the temperature of the RTO discharge gas. Adjusting the temperature of the gas discharged from the regenerative thermal oxidizer to the above temperature range makes it possible to control the temperature to a temperature suitable for catalyst regeneration in the second reactor described below, and to control the hot spot of the catalyst to an appropriate temperature during the coke combustion process. Preferably, the gas can be discharged at 150 to 450℃, 200 to 400℃, or 250 to 350℃. Meanwhile, the steam generator is a heat exchanger that receives a heat supply from a high-temperature heat source (the gas discharged from the regenerative thermal oxidizer) and boils BFW (boiling feed water) to generate steam. Thereby, the gas discharged from the regenerative thermal oxidizer can be cooled to reduce its temperature to an appropriate level.

[0051] Meanwhile, the gas discharged from the above regenerative thermal oxidizer is added to the second reactor of the present application. The second reactor of the present application is a reactor in the form of a catalyst packing after the completion of the lactic acid dehydration reaction, which is a reactor in which coke is formed on the catalyst layer inside the reactor. In a conventional catalyst regeneration process, a gas stream containing only inert gas and oxygen is added to the reactor to perform the catalyst regeneration process as described above, however, in the present disclosure, byproduct treatment and catalyst regeneration can be efficiently performed by using the above regenerative thermal oxidizer.

[0052] According to one embodiment, the second reactor can be operated at 300 to 500℃. If the temperature of the second reactor is too high, there can be a problem of shortening the catalyst life due to thermal shock, and if the temperature is too low, there can be a problem of reducing the efficiency of coke removal. Preferably, the temperature of the second reactor can be 300℃ or more, 330℃ or more, 350℃ or more, and 500℃ or less, 480℃ or less, 460℃ or less. At the same time, the temperature of the catalyst layer can be controlled in the same range by controlling the operating temperature of the second reactor.

[0053] Further, the catalyst regeneration step can be configured in the form of a swing reactor, which converts the first reactor into the second reactor when the yield of acrylic acid after the lactic acid dehydration reaction in the first reactor is reduced by 5 to 20% or 10 to 20% relative to normal operation.

[0054] At the same time, according to the present disclosure, there is provided an apparatus for regeneration of a fixed bed catalytic reactor, the apparatus comprising: a first reactor 100 of a fixed bed isothermal type filled with a catalyst; a separator that separates the product of the first reactor; a regeneration thermal oxidizer that burns by-products discharged from the upper portion of the separator; and a second reactor of a fixed bed isothermal type in which a catalyst is filled and to which a gas discharged from the regeneration thermal oxidizer is supplied.

[0055] Details of the first reactor, the separator, the regeneration thermal oxidizer, and the second reactor are as described above. Further, if necessary, the apparatus can further include a heat exchanger that cools the gas discharged from the regeneration thermal oxidizer and supplies it to the second reactor.

[0056] Figure 1 is a process diagram schematically showing a method according to one aspect of the present disclosure.

[0057] Reference Figure 1 It can be confirmed that the method for regenerating a fixed bed catalytic reactor according to one aspect of the present disclosure includes a series of steps: a step of supplying a feed 110 containing lactic acid gas to a first reactor 100 filled with a catalyst to perform a lactic acid dehydration reaction; a step of separating acrylic acid and by-products 220 from the reaction product 120; a step of adding the by-products to a regeneration thermal oxidizer (RTO) 500; and a step of adding a gas discharged from the regeneration thermal oxidizer to a second reactor 700 filled with a catalyst to regenerate the catalyst.

[0058] Further, with reference to Figure 1It can be confirmed that the apparatus for regeneration of a fixed bed catalytic reactor according to one aspect of the disclosure includes a first reactor 100 of a fixed bed isothermal type filled with a catalyst, a separator 200 that separates a product of the first reactor, a regeneration thermal oxidizer 500 that burns by-products discharged from the upper portion of the separator, and a second reactor 700 of a fixed bed isothermal type in which a catalyst is filled and a gas discharged from the regeneration thermal oxidizer is supplied.

[0059] In addition, as needed, the acrylic acid production apparatus of the present disclosure can further include a compressor 300 and a gas-liquid separator 400. In addition, the acrylic acid production apparatus of the present disclosure can further include a heat exchanger 600 that cools a gas discharged from the regeneration thermal oxidizer 500 and supplies it to the second reactor 700, wherein the heat exchanger can be a steam generator.

[0060] [Advantageous Effects]

[0061] As described above, the regeneration method and apparatus of a fixed bed catalytic reactor according to the present disclosure can regenerate a catalyst using a gas discharged from a regeneration thermal oxidizer, thereby reducing process costs, minimizing thermal shock of the catalyst, and achieving stable regeneration. BRIEF DESCRIPTION OF DRAWINGS

[0062] Figure 1 is a process diagram schematically showing a method according to one aspect of the disclosure.

[0063] Figure 2 is a process diagram schematically showing a catalyst regeneration apparatus according to a comparative example. DETAILED DESCRIPTION

[0064] Hereinafter, preferred embodiments are provided to better understand the present disclosure. However, these embodiments are for illustrative purposes only, and the present disclosure is not intended to be limited by these embodiments.

[0065] Example 1

[0066] As Figure 1 shown, a 40 wt.% aqueous lactic acid solution was evaporated at 350℃ and added to the first reactor, and a dehydration reaction was performed to produce a reaction product containing acrylic acid (acrylic acid 17.0 wt.%, by-products: acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide and carbon monoxide, etc., total 10 wt.%).

[0067] Then, the reaction product is supplied to a separator to separate low-boiling substances and high-boiling substances in the reaction product. A cooling tower is used as the separator. In the cooling tower, low-boiling by-products (acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide) contained in the reaction product are discharged to the upper portion of the cooling tower together with nitrogen contained in the reaction product, and acrylic acid is discharged to the lower portion together with high-boiling substances. The stream discharged to the upper portion of the cooling tower is compressed by a compressor, and condensate and gas-phase substances are separated in a gas-liquid separator.

[0068] Then, the gas-phase substances (acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide) discharged from the gas-liquid separator are added to a regenerative thermal oxidizer (RTO) together with air. The regenerative thermal oxidizer operates at a temperature of about 800°C, and a gas containing nitrogen, carbon dioxide, water, and oxygen is discharged by complete combustion. Steam is generated in a heat exchanger (steam generator) using the discharge gas at about 800°C, and then cooled to 350°C (oxygen concentration: 3.5 vol%). Then, the cooled regenerative thermal oxidizer discharge stream is added to a second reactor for catalyst regeneration, in which coke produced during the reaction is accumulated on the catalyst layer (at the point at which the acrylic acid yield is reduced by 10%) in the second reactor. The second reactor is allowed to regenerate the catalyst for 24 hours while maintaining the temperature at 400°C.

[0069] Example 2

[0070] The dehydration reaction was performed in the same manner as in Example 1, and gas-phase substances were obtained by a cooling tower and a gas-liquid separator. The gas-phase substances discharged from the gas-liquid separator were added to a regenerative thermal oxidizer (RTO) together with air. The regenerative thermal oxidizer operates at a temperature of about 700°C, and a gas containing nitrogen, carbon dioxide, water, and oxygen is discharged by complete combustion. Steam was generated in a heat exchanger (steam generator) using the discharge gas at about 700°C, and then cooled to 390°C (oxygen concentration: 0.5 vol%). Then, the cooled regenerative thermal oxidizer discharge stream was added to a second reactor for catalyst regeneration, in which coke produced during the reaction was accumulated on the catalyst layer (at the point at which the acrylic acid yield was reduced by 10%) in the second reactor. The second reactor regenerated the catalyst for 24 hours while maintaining the temperature at 400°C.

[0071] Example 3

[0072] The dehydration reaction was carried out in the same manner as in Example 1, and a gaseous substance was obtained through a cooling tower and a gas-liquid separator. The gaseous substance discharged from the gas-liquid separator was added to a regenerative thermal oxidizer (RTO) along with air. The RTO operated at a temperature of approximately 600°C, and the gas containing nitrogen, carbon dioxide, water, and oxygen was discharged through complete combustion. After steam was generated in a heat exchanger (steam generator), the exhaust gas at approximately 600°C was cooled to 400°C (oxygen concentration: 0.5 vol%). Then, to increase the oxygen concentration of the cooled RTO exhaust stream, air at 25°C was added to the stream, and a regenerative stream with an oxygen concentration of 2.0 vol% at 370°C was prepared.

[0073] The regenerated stream was added to the second reactor for catalyst regeneration, in which coke generated during the reaction accumulated on the catalyst bed (catalyst at the point where acrylic acid yield decreased by 10%). The catalyst in the second reactor was regenerated for 24 hours while maintaining the temperature at 400°C.

[0074] Comparative example

[0075] The second reactor was prepared under the same conditions as in the previous example. As follows. Figure 2 As shown, a separate regeneration gas stream was prepared for catalyst regeneration. Specifically, air and nitrogen were mixed at a volume ratio of 1:5 to prepare a regeneration gas with an oxygen concentration of 3.5% by volume. The prepared regeneration gas was heated to 350°C in a flame heater and then added to a second reactor. The catalyst was regenerated in the second reactor for 24 hours while maintaining the temperature at 400°C.

[0076] The comparative production method, which involves preparing and adding a separate regeneration stream, can lead to the following problems: increased catalyst regeneration costs due to the consumption of nitrogen to produce regeneration gas with a suitable oxygen concentration (3.5 vol%) and temperature (350°C) and the use of LNG fuel in the flame heater. On the other hand, the method for producing acrylic acid according to this disclosure provides excellent process economy and enables stable catalyst regeneration by treating the waste gas and / or waste oil generated as byproducts after the production of acrylic acid from lactic acid through a regenerating combustion oxidizer and then using the exhaust gas stream for catalyst regeneration.

[0077] [Symbol Explanation]

[0078] 100: First reactor

[0079] 110: Feeding

[0080] 120: Reaction product

[0081] 200: Separator

[0082] 220: by-product

[0083] 300: compressor

[0084] 400: gas-liquid separator

[0085] 500: regenerative thermal oxidizer (RTO)

[0086] 600: heat exchanger

[0087] 700: second reactor

[0088] 800: compressor

[0089] 810: gas stream

[0090] 820: nitrogen stream

[0091] 900: flame heater

[0092] 910: fuel supply unit

Claims

1. A method of regenerating a fixed bed catalytic reactor, the method comprising the steps of: supplying a feed containing lactic acid gas into a first reactor filled with a catalyst to perform a lactic acid dehydration reaction; separating acrylic acid and by-products from a reaction product; adding the by-products into a regenerative thermal oxidizer (RTO); and adding a gas discharged from the regenerative thermal oxidizer into a second reactor filled with a catalyst to regenerate the catalyst.

2. The method of regenerating a fixed bed catalytic reactor of claim 1, wherein, The reaction product contains 5 to 30 wt% of acrylic acid and 1 to 15 wt% of by-products other than water.

3. The method of regenerating a fixed bed catalytic reactor of claim 1, wherein, The by-products added into the regenerative thermal oxidizer include at least one selected from the group consisting of acetaldehyde, 2-pentanedione, lactic acid, carbon dioxide, and carbon monoxide.

4. The method of regenerating a fixed bed catalytic reactor of claim 1, wherein, The regenerative thermal oxidizer is operated at a temperature condition of 300 to 900℃.

5. The method of regenerating a fixed bed catalytic reactor of claim 1, wherein, The gas discharged from the regenerative thermal oxidizer contains 0.5 to 10 vol% of oxygen. 6.The method of regenerating a fixed bed catalytic reactor according to claim 1, further comprising controlling a temperature of the gas discharged from the regenerative thermal oxidizer to be 100 to 500℃.

7. The method of regenerating a fixed bed catalytic reactor of claim 1, wherein, The second reactor is operated at 300 to 500℃. 8.An apparatus for regenerating a fixed bed catalytic reactor, the apparatus comprising: a first reactor of a fixed bed isothermal type filled with a catalyst; a separator that separates a product of the first reactor; a regenerative thermal oxidizer that burns by-products discharged from an upper portion of the separator; and a second reactor of a fixed bed isothermal type filled with a catalyst and supplied with a gas discharged from the regenerative thermal oxidizer. 9.The apparatus for regenerating a fixed bed catalytic reactor according to claim 8, further comprising a heat exchanger that cools the gas discharged from the regenerative thermal oxidizer and supplies it to the second reactor.

10. The apparatus for regenerating a fixed bed catalytic reactor of claim 9, wherein, The heat exchanger is a steam generator.

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