Method and apparatus for regeneration of fixed bed catalytic reactor

Abstract

The present invention relates to a method and an apparatus for the regeneration of a fixed bed catalytic reactor, and more specifically, to a method and an apparatus for the regeneration of a catalyst during the production of acrylic acid from lactic acid.

Description

Fixed-bed catalytic reactor regeneration method and regeneration device

[0001] Cross-citation with related application(s)

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

[0003]

[0004] The present invention relates to a fixed bed catalyst reactor regeneration method and regeneration device, and to a catalyst regeneration method and regeneration device for producing acrylic acid from lactic acid.

[0005]

[0006] Acrylic acid is an organic compound that contains both carboxylic acid and an unsaturated double bond within its molecule. It has a very simple structure, can be converted into various substances, and can be polymerized, so it is used in various industrial fields.

[0007]

[0008] Specifically, acrylic acid can be used as polyacrylic acid, dots, adhesives, paints, etc. required for manufacturing superabsorbent polymers, or as a raw material for manufacturing other types of acrylate monomers, or as a polymerization raw material with various other monomers such as acrylamide, acrylonitrile, styrene, and alpha olefins.

[0009] These acrylic acids are usually manufactured using propylene produced during the refining and separation process of crude oil, such as naphtha cracking.

[0010]

[0011] However, with the recent increase in concerns about crude oil depletion and environmental issues, interest in methods for producing acrylic acid using environmentally friendly raw materials is growing.

[0012]

[0013] The present invention aims to provide a fixed bed catalyst reactor regeneration method and regeneration device capable of stably regenerating a catalyst while reducing catalyst regeneration costs.

[0014]

[0015] In order to solve the above problem, the present invention provides a method for regenerating a fixed bed catalytic reactor, comprising 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 the reaction product; introducing the by-products into a regenerative thermal oxidizer (RTO); and introducing a gas discharged from the regenerative thermal oxidizer into a second reactor filled with a catalyst to regenerate the catalyst.

[0016]

[0017] In one example, the reaction product may comprise 5 to 30 wt% acrylic acid and 1 to 15 wt% by-products other than water.

[0018]

[0019] According to one example, the byproducts fed into the regenerative combustion oxidizer may include at least one selected from the group consisting of acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide.

[0020]

[0021] In one example, the regenerative combustion oxidizer can be operated at a temperature condition of 300 to 900°C.

[0022]

[0023] In one example, the gas discharged from the regenerative combustion oxidizer may contain 0.5 to 10 volume percent oxygen.

[0024]

[0025] According to one example, the method may further include a step of controlling the temperature of the gas discharged from the regenerative combustion oxidizer to 100 to 500°C.

[0026]

[0027] In one example, the second reactor can be operated at 300 to 500°C.

[0028]

[0029] In addition, the present invention provides a fixed-bed catalytic reactor regeneration device comprising: a first reactor of a fixed-bed isothermal type filled with a catalyst; a separator for separating a product of the first reactor; a regenerative combustion oxidizer for combusting byproducts 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 combustion oxidizer.

[0030]

[0031] In one example, the regenerative combustion oxidizer may further include a heat exchanger that cools the gas discharged therefrom and supplies it to the second reactor. In addition, the heat exchanger may be a steam generator.

[0032]

[0033] In the present invention, terms such as first, second, etc. are used to describe various components, and the terms are used only for the purpose of distinguishing one component from another.

[0034] Additionally, the terms used herein are merely used to describe exemplary embodiments and are not intended to limit the present invention.

[0035] Singular expressions include plural expressions unless the context clearly indicates otherwise.

[0036] In this specification, the terms “comprise,” “include,” or “have” are intended to describe a feature, number, step, component, or combination thereof implemented, but do not exclude the possibility of one or more other features, numbers, steps, components, combinations, or additions thereof.

[0037] Additionally, in this specification, when each layer or element is referred to as being formed “on” or “over” each layer or element, it means that each layer or element is formed directly on each layer or element, or that other layers or elements may be additionally formed between each layer, on the object, or on the substrate.

[0038] The present invention is susceptible to various modifications and takes various forms. Specific embodiments are illustrated and described in detail below. However, this does not limit the invention to a specific disclosed form, but rather encompasses all modifications, equivalents, and alternatives falling within the spirit and technical scope of the present invention.

[0039]

[0040] Hereinafter, the present invention will be described in detail.

[0041]

[0042] According to one aspect of the present invention, a method for regenerating a fixed bed catalytic reactor is provided, comprising: 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 the reaction product; introducing the by-products into a regenerative thermal oxidizer (RTO); and introducing a gas discharged from the regenerative thermal oxidizer into a second reactor filled with a catalyst to regenerate the catalyst.

[0043]

[0044] The process for producing acrylic acid through the gas-phase dehydration of lactic acid is primarily conducted under acid catalysis. During this process, olefin compounds, such as the reactant lactic acid, the product acrylic acid, and intermediates, are present, frequently forming coke on the catalyst surface. This coke can block the catalyst's active sites, leading to catalyst deactivation. Furthermore, the accumulated coke can rapidly increase the differential pressure between the catalyst bed, potentially halting the process. Consequently, excessive coke precipitated in the catalyst bed inhibits the yield of the desired product, acrylic acid.

[0045]

[0046] Therefore, the catalyst used in the method for producing acrylic acid via lactic acid gas phase dehydration requires a regeneration process to remove the coke formed in the catalyst layer. Coke is a carbon deposit. To remove coke, reactor operation is typically halted and oxygen-containing air is injected to combust the coke. This coke combustion reaction is exothermic, forming hot spots on the catalyst. This can lead to catalyst sintering during regeneration at high temperatures.

[0047]

[0048] Thus, during the acrylic acid production process via lactic acid gas phase dehydration, controlling the catalyst hot spot temperature is crucial during the catalyst regeneration process. To control the hot spot temperature during catalyst regeneration, an inert gas is typically used alongside oxygen to lower the oxygen partial pressure. Nitrogen, which is primarily used as an inert gas, increases process costs if added separately during regeneration.

[0049]

[0050] Accordingly, the inventors of the present invention have completed the present invention by confirming that the process cost can be reduced by using the gas discharged from a regenerative combustion oxidizer for by-product treatment after acrylic acid production as a high-temperature inert gas in order to reduce the cost of the regeneration process.

[0051]

[0052] First, there is no particular limitation on the method for producing a feed containing lactic acid gas, which is a reactant of the present invention, and it can be produced by a method conventional in the art, but as an example, the method described below can be applied.

[0053]

[0054] The above lactic acid gas can be produced by vaporizing an aqueous lactic acid solution. The aqueous lactic acid solution may preferably have a concentration range of about 10 to about 80 wt%.

[0055] If the concentration of lactic acid is too low, the efficiency of the vaporization step and the efficiency of the dehydration reaction in the first step may be too low, and if the concentration of lactic acid is too high, the content of oligomers, etc. in the aqueous solution may increase, which may lower the efficiency of the dehydration reaction and promote the production of by-products.

[0056]

[0057] In addition, the vaporization reaction of lactic acid can proceed under temperature conditions of about 200°C to 300°C. If the temperature of the vaporization reaction is too low, the vaporization efficiency may decrease, and if the temperature of the vaporization reaction is too high, the decarboxylation or decarbonylation reaction of the vaporized lactic acid molecules may proceed predominantly, which may cause a problem of promoting the production of aldehyde.

[0058]

[0059] Next, a feed containing lactic acid gas can be supplied to a reactor filled with a catalyst to perform a lactic acid dehydration reaction.

[0060] The feed containing the above lactic acid gas can be continuously supplied to a catalyst section where a catalyst is present according to the flow of carrier gas. The carrier gas is an inert gas, such as nitrogen.

[0061]

[0062] Additionally, the above reaction may proceed at a temperature of about 300° C. to about 400° C. If the reaction temperature is too low, the lactic acid conversion rate and acrylic acid yield may decrease, and if the reaction temperature is too high, the amount of byproducts produced may increase.

[0063]

[0064] In addition, the catalyst may include at least one selected from the group consisting of a calcium phosphate-based catalyst, a sodium phosphate-based catalyst, and an aluminum phosphate-based catalyst, and other reaction conditions may be used without particular limitation as long as they are generally used in the technical field to which the present invention pertains, as long as they do not conflict with the contents limited in the present specification. For example, the catalyst may include CaSO4 / Na2SO4; Na4P2O7 / CaSO4; Na4P2O7 / Ca3(PO4)2; NaH2PO4-NaHCO3 / SiO2; AlPO4-NH3; Ca3(PO4)2 / CaSO4; Ca2P2O7; Ca5(PO4)3(OH), etc.

[0065]

[0066] In addition, according to an example, the manufacturing method may be a batch type or a continuous type, but it is preferably a continuous type equipped with a catalyst layer in which lactic acid gas for reaction is continuously transferred to the reactor and acrylic acid, which is a product of the dehydration reaction, is also continuously obtained.

[0067]

[0068] In one example, the reaction product may comprise 5 to 30 wt% acrylic acid and 1 to 15 wt% by-products other than water. Preferably, the reaction product may comprise 8 to 28 wt%, or 10 to 25 wt%, acrylic acid and 3 to 12 wt%, or 5 to 10 wt% by-products other than water.

[0069]

[0070] During the lactic acid dehydration reaction, byproducts such as acrylic acid and side reactions may be produced. These byproducts may include, in addition to acrylic acid, water, acetaldehyde, carbon monoxide, carbon dioxide, dilution gases, low-boiling point byproducts, high-boiling point byproducts, and unreacted lactic acid. Therefore, after the lactic acid dehydration reaction described above, a step is performed to separate the desired product, acrylic acid, and the byproducts from the reaction products formed.

[0071]

[0072] The step of separating acrylic acid and by-products can utilize processes commonly used in the art. For example, the reaction product stream can be fed to a cooling tower for condensation, and then the effluent stream containing acrylic acid can be fed to a distillation tower for distillation to separate acrylic acid and by-products. Alternatively, the reaction product can be condensed in multiple cooling towers, and then acrylic acid and by-products can be separated in an extraction tower using an extractant.

[0073]

[0074] Additionally, if necessary, the above process may further include additional devices such as heat exchangers, valves, pumps, separators, and mixers.

[0075]

[0076] The present invention includes a step of introducing a byproduct separated from the reaction product containing the acrylic acid into a regenerative thermal oxidizer (RTO). Generally, a regenerative thermal oxidizer refers to a device that stores waste heat of exhaust gas through direct contact, reuses the stored heat, and incinerates and removes volatile organic compound gases generated in the process. The regenerative thermal oxidizer may include a combustion chamber and a predetermined number of beds made of a regenerative material to increase the heat recovery rate.

[0077]

[0078] According to one example, the by-products fed into the regenerative combustion oxidizer may include at least one selected from the group consisting of acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide.

[0079]

[0080] According to an example, the regenerative combustion oxidizer can be operated under a temperature condition of 300 to 900°C. If the temperature is less than 300°C, complete combustion may not occur, and if it exceeds 900°C, there may be a problem of heat damage to the regenerative combustion oxidizer. Preferably, the regenerative combustion oxidizer can be operated under a temperature condition of 300 to 900°C, 400 to 850°C, or 500 to 800°C. Meanwhile, by operating the regenerative combustion oxidizer at a temperature in the above range, the temperature of the gas discharged from the regenerative combustion oxidizer can be controlled within the above-described range.

[0081]

[0082] Additionally, according to one example, the gas discharged from the regenerative combustion oxidizer may contain oxygen in an amount of 0.5 to 10% by volume. Including oxygen in the above range provides an oxygen partial pressure suitable for catalyst regeneration in the second reactor described below, thereby allowing the hot spot of the catalyst to be controlled at an appropriate temperature during the coke combustion process. Preferably, the gas may contain oxygen in an amount of 0.5 to 10% by volume, 1 to 8% by volume, or 2 to 5% by volume.

[0083] Additionally, the gas discharged from the regenerative combustion oxidizer may further include nitrogen, carbon dioxide, carbon monoxide, water, etc. in addition to oxygen.

[0084]

[0085] According to one example, the method may further include a step of controlling the temperature of the gas discharged from the regenerative combustion oxidizer to 100 to 500°C. For example, the step may be performed by introducing the gas discharged from the regenerative combustion oxidizer into a steam generator to generate steam through heat exchange, and controlling the temperature of the RTO exhaust gas. Controlling the temperature of the gas discharged from the regenerative combustion oxidizer to the above-described temperature range makes it possible to control the hot spot of the catalyst to an appropriate temperature during the coke combustion process at a temperature suitable for catalyst regeneration in the second reactor described below. Preferably, the gas may be discharged at 150 to 450°C, 200 to 400°C, or 250 to 350°C. Meanwhile, the steam generator is a heat exchanger that receives heat from a high-temperature heat source (the gas discharged from the regenerative combustion oxidizer) and boils BFW (Boiling Feed Water) to create steam. Through this, the gas discharged from the regenerative combustion oxidizer can be cooled to lower the temperature to an appropriate level.

[0086]

[0087] Meanwhile, the gas discharged from the above-described regenerative combustion oxidizer is fed into the second reactor of the present invention. The second reactor of the present invention is a reactor filled with a catalyst, in which a lactic acid dehydration reaction has been performed, and in which coke has been formed in the catalyst layer within the reactor. As described above, the conventional catalyst regeneration process involves feeding a separate inert gas and oxygen-containing gas stream into the reactor to undergo the catalyst regeneration process. However, the present invention utilizes the regenerative combustion oxidizer to efficiently process by-products and regenerate the catalyst.

[0088]

[0089] In one example, the second reactor may be operated at 300 to 500°C. If the temperature of the second reactor is too high, there may be a problem of shortening the catalyst life due to thermal shock, and if it is too low, there may be a problem of reduced coke removal efficiency. Preferably, the temperature of the second reactor may be 300°C or higher, 330°C or higher, or 350°C or higher, and 500°C or lower, 480°C or lower, or 460°C or lower. Meanwhile, the temperature of the catalyst layer may be controlled within the same range by controlling the operating temperature of the second reactor.

[0090]

[0091] In addition, the catalyst regeneration step may be configured in the form of a swing reactor that switches the first reactor to the second reactor when the yield of acrylic acid decreases by 5 to 20% or 10 to 20% compared to normal operation after the lactic acid dehydration reaction is performed in the first reactor.

[0092]

[0093] Meanwhile, the present invention provides a fixed-bed catalytic reactor regeneration device comprising: a first reactor of a fixed-bed isothermal type filled with a catalyst; a separator for separating a product of the first reactor; a regenerative combustion oxidizer for combusting byproducts discharged to 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 combustion oxidizer.

[0094]

[0095] The description of the first reactor, separator, regenerative combustion oxidizer, and second reactor is as described above. In addition, if necessary, a heat exchanger may be further included to cool the gas discharged from the regenerative combustion oxidizer and supply it to the second reactor.

[0096]

[0097] Figure 1 is a process diagram schematically showing a method according to one aspect of the present invention.

[0098] Referring to FIG. 1, in a fixed bed catalytic reactor regeneration method according to one aspect of the present specification, a series of processes can be confirmed, including 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 a by-product (220) from the reaction product (120); a step of introducing the by-product into a regenerative thermal oxidizer (RTO (500)); and a step of introducing a gas discharged from the regenerative thermal oxidizer into a second reactor (700) filled with a catalyst to regenerate the catalyst.

[0099]

[0100] Also, referring to FIG. 1, a fixed-bed catalytic reactor regeneration device can be confirmed, which includes a first reactor (100) of a fixed-bed isothermal type filled with a catalyst according to one aspect of the present invention; a separator (200) for separating a product of the first reactor; a regenerative combustion oxidizer (500) for combusting byproducts discharged to the upper portion of the separator; and a second reactor (700) of a fixed-bed isothermal type filled with a catalyst and supplied with gas discharged from the regenerative combustion oxidizer.

[0101] In addition, the acrylic acid production device of the present invention may further include a compressor (300) and a gas-liquid separator (400), if necessary. In addition, the acrylic acid production device of the present invention may further include a heat exchanger (600) that cools the gas discharged from the regenerative combustion oxidizer (500) and supplies it to the second reactor (700), and the heat exchanger may be a steam generator.

[0102]

[0103] As described above, according to the fixed bed catalyst reactor regeneration method and regeneration device of the present invention, the catalyst is regenerated using gas discharged from a regenerative combustion oxidizer, thereby reducing process costs and minimizing thermal shock to the catalyst, thereby enabling stable regeneration.

[0104]

[0105] Figure 1 is a process diagram schematically showing a method according to one aspect of the present invention.

[0106] Figure 2 is a process diagram schematically showing a catalyst regeneration device of a comparative example.

[0107]

[0108] Hereinafter, preferred embodiments are presented to aid understanding of the invention. However, the following examples are intended only to illustrate the invention and are not intended to limit the invention to these embodiments.

[0109]

[0110] Example 1

[0111] As shown in Figure 1 below, a 40 wt% lactic acid aqueous solution was vaporized at 350°C and introduced into the first reactor, and a reaction product including acrylic acid was produced through a dehydration reaction (17.0 wt% acrylic acid, by-products: acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide, totaling 10 wt%).

[0112]

[0113] Afterwards, the reaction product was supplied to a separator to separate low-boiling-point substances and high-boiling-point substances in the reaction product. A cooling tower was used as the separator. In the cooling tower, low-boiling-point by-products (acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide) contained in the reaction product were discharged to the top of the cooling tower together with the nitrogen contained in the reactant, and acrylic acid was discharged to the bottom of the cooling tower together with the high-boiling-point substances. The stream discharged to the top of the cooling tower was compressed using a compressor, and the condensed substance and the gaseous substance were separated in a gas-liquid separator.

[0114]

[0115] Afterwards, the gaseous substances (acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide) discharged from the gas-liquid separator were fed into a regenerative thermal oxidizer (RTO) together with air. The regenerative thermal oxidizer was operated at a temperature of approximately 800°C and discharged gases including nitrogen, carbon dioxide, water, and oxygen through complete combustion. The exhaust gas at approximately 800°C was cooled to 350°C after generating steam in a heat exchanger (steam generator) (oxygen concentration 3.5 vol%). Afterwards, the cooled regenerative thermal oxidizer discharge stream was fed to the second reactor for catalyst regeneration where the coke generated during the reaction was accumulated on the catalyst layer (the catalyst at the point where the yield of acrylic acid was reduced by 10%). The second reactor was regenerated for 24 hours while maintaining the temperature at 400°C.

[0116]

[0117] Example 2

[0118] 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 fed into a regenerative thermal oxidizer (RTO) together with air. The regenerative thermal oxidizer was operated at a temperature of approximately 700°C and discharged gases including nitrogen, carbon dioxide, water, and oxygen through complete combustion. The exhaust gas at approximately 700°C was cooled to 390°C after generating steam in a heat exchanger (steam generator) (oxygen concentration 0.5 vol%). Thereafter, the cooled regenerative thermal oxidizer discharge stream was fed to the second reactor for catalyst regeneration where the coke generated during the reaction was accumulated on the catalyst layer (the catalyst at the point where the yield of acrylic acid decreased by 10%). The second reactor regenerated the catalyst for 24 hours while maintaining the temperature at 400°C.

[0119]

[0120] Example 3

[0121] 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 fed into a regenerative thermal oxidizer (RTO) together with air. The regenerative thermal oxidizer was operated at a temperature of approximately 600°C and discharged gases including nitrogen, carbon dioxide, water, and oxygen through complete combustion. The exhaust gas at approximately 600°C was cooled to 400°C after generating steam in a heat exchanger (steam generator) (oxygen concentration 0.5 vol%). Thereafter, in order to increase the oxygen concentration of the cooled regenerative thermal oxidizer exhaust stream, air at 25°C was injected into the stream, thereby producing a regeneration stream with an oxygen concentration of 2.0 vol% and a temperature of 370°C.

[0122] The above regeneration stream was introduced for catalyst regeneration in the second reactor where coke generated during the reaction was accumulated on the catalyst layer (catalyst at the point where the yield of acrylic acid was reduced by 10%). The catalyst in the second reactor was regenerated for 24 hours while maintaining the temperature at 400°C.

[0123]

[0124] Comparative example

[0125] A second reactor was prepared in the same condition as the example, and a separate regeneration gas stream was prepared for catalyst regeneration as shown in Fig. 2 below. Specifically, air and nitrogen were mixed in 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 fired heater and then introduced into the second reactor. The catalyst was regenerated in the second reactor for 24 hours while maintaining the temperature at 400°C.

[0126]

[0127] The comparative manufacturing method of manufacturing and injecting a separate regeneration stream may have a problem in that the cost of catalyst regeneration increases due to the nitrogen consumed to manufacture the regeneration gas with an appropriate oxygen concentration (3.5 volume%) and temperature (350°C) and the LNG fuel used in the fired heater. On the other hand, the method for manufacturing acrylic acid according to the present invention described above performs catalyst regeneration using the gas stream discharged after treating waste gas and / or waste oil generated as a by-product after manufacturing acrylic acid from lactic acid through a regenerative combustion oxidizer, thereby providing excellent process economics and enabling stable regeneration of the catalyst.

[0128]

[0129] [Explanation of symbols]

[0130] 100: First reactor 110: Feed

[0131] 120: Reaction product 200: Separator

[0132] 220: By-product 300: Compressor

[0133] 400: Gas-liquid separator 500: Regenerative thermal oxidation (RTO)

[0134] 600: Heat exchanger 700: Second reactor

[0135] 800: Compressor 810: Air stream

[0136] 820: Nitrogen stream 900: Fired heater

[0137] 910: Fuel Supply

Claims

1. A step of supplying a feed containing lactic acid gas to a first reactor filled with a catalyst to perform a lactic acid dehydration reaction; A step of separating acrylic acid and by-products from the above reaction product; A step of feeding the above by-product into a regenerative thermal oxidizer (RTO); and A step of regenerating the catalyst by injecting the gas discharged from the regenerative combustion oxidizer into a second reactor filled with a catalyst, Method for regenerating a fixed bed catalytic reactor.

2. In paragraph 1, The reaction product comprises 5 to 30 wt% of acrylic acid and 1 to 15 wt% of by-products other than water. Method for regenerating a fixed bed catalytic reactor.

3. In paragraph 1, The by-products fed into the above regenerative combustion oxidizer include at least one selected from the group consisting of acetaldehyde, 2,3-pentanedione, lactic acid, carbon dioxide, and carbon monoxide. Method for regenerating a fixed bed catalytic reactor.

4. In paragraph 1, The above accumulator combustion oxidizer is operated under temperature conditions of 300 to 900 ℃. Method for regenerating a fixed bed catalytic reactor.

5. In paragraph 1, The gas discharged from the above accumulator contains oxygen at 0.5 to 10 volume%. Method for regenerating a fixed bed catalytic reactor.

6. In paragraph 1, Further comprising a step of controlling the temperature of the gas discharged from the above accumulator-type combustion oxidizer to 100 to 500°C. Method for regenerating a fixed bed catalytic reactor.

7. In paragraph 1, The second reactor is operated at 300 to 500°C. Method for regenerating a fixed bed catalytic reactor.

8. First reactor of fixed bed isothermal type filled with catalyst; A separator for separating the product of the first reactor; A regenerative combustion oxidizer that burns the byproducts discharged from the upper portion of the above separator; and A second reactor having a fixed bed isothermal type, which is filled with a catalyst inside and is supplied with gas discharged from the regenerative combustion oxidizer. Fixed bed catalytic reactor regeneration device.

9. In paragraph 8, Further comprising a heat exchanger for cooling the gas discharged from the regenerative combustion oxidizer and supplying it to the second reactor. Fixed bed catalytic reactor regeneration device.

10. In paragraph 9, The above heat exchanger is a steam generator, Fixed bed catalytic reactor regeneration device.

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