Self-heat exchange type hydrogenation reactor and hydrogenation method thereof

Abstract

This invention provides a self-heating hydrogenation reactor and its hydrogenation method, relating to the field of reactor design technology. The reactor includes a shell and a catalyst bed disposed inside the shell. The shell includes a feed section, a reaction section, and a collection section. The reaction section includes an outer ring bed and a core bed, both filled with catalyst, with the outer ring bed surrounding the periphery of the core bed. By coupling the core bed and the outer ring bed within the same shell, heat exchange between the core bed and the outer ring bed streams is achieved solely through the heat of the hydrogenation reaction, ultimately maintaining the required reaction temperature. Compared to conventional hydrogenation units, this eliminates the need for a feed preheating system and a cold hydrogen circulation system, reducing energy consumption and investment costs.

Description

Technical Field

[0001] This invention relates to the field of reactor design technology, specifically to a self-heating hydrogenation reactor and its hydrogenation method. Background Technology

[0002] Innovative reactor design is of significant practical importance for hydrogenation reactions. Currently, some novel reactors with reaction-enhancing capabilities (such as microreactors) are being used on a laboratory scale. Industrially, hydrogenation reactors are mostly fixed-bed reactors, designed to achieve low cost, low catalyst packing volume, high conversion rate, low byproducts, and high heat recovery. Therefore, the effective removal and utilization of reaction heat is one of the key factors in reactor design. Since catalytic hydrogenation is an exothermic reaction, the temperature of the reactants needs to be controlled during its preparation to meet the requirements of subsequent processes.

[0003] In existing technologies, most hydrogenation processes involve preheating the feedstock before mixing it with hydrogen gas and then introducing it into the reactor for the hydrogenation reaction. To prevent reactor overheating, a cold hydrogen device is often installed inside the reactor. This involves injecting a large amount of cold hydrogen to remove excess reaction heat and prevent localized overheating, thereby controlling the reaction temperature. However, the large amount of cold hydrogen injected is only used to remove the heat of the hydrogenation reaction and does not participate in the internal catalytic hydrogenation reaction. This results in a large consumption of cold hydrogen, low utilization rate, and increased operating costs of the entire catalytic hydrogenation unit. Summary of the Invention

[0004] The purpose of this invention is to provide a self-heating hydrogenation reactor and its hydrogenation method, so as to alleviate the technical problems existing in the prior art, such as low utilization rate, large consumption of cold hydrogen, and high operating cost of the device because a large amount of hydrogen injected into the reactor does not directly participate in the reaction.

[0005] In a first aspect, the self-heating hydrogenation reactor provided by the present invention includes a shell, the shell including a feed section, a reaction section and a collection section, the reaction section including an outer ring bed and a core bed, the interior of the core bed and the interior of the outer ring bed are both filled with catalyst, and the outer ring bed is arranged around the periphery of the core bed;

[0006] The collecting section includes a first chamber and a second chamber. The first chamber is connected to the core bed, and the second chamber is connected to the outer ring bed.

[0007] The first chamber is provided with a liquid circulation outlet, which is connected to the outer ring bed;

[0008] The shell also includes a feeding section, which is located at the upper part of the shell, and the reaction section is connected between the feeding section and the collecting section.

[0009] Preferably, the outer ring bed is provided with a plurality of connecting pipes, which are wound and installed around the periphery of the inner core bed, and the connecting pipes are corrugated pipes.

[0010] Preferably, the bottom of the collecting section is provided with a partition, which is used to divide the collecting section into a first chamber and a second chamber.

[0011] Preferably, the collecting section further includes a guide tube and a liquid circulation outlet. The guide tube is connected between the core bed and the collecting section, and the end of the guide tube facing the collecting section extends along the first chamber. The liquid circulation outlet is located at the bottom of the first chamber.

[0012] Preferably, the collecting section further includes a baffle and a product outlet. The baffle is disposed between the outer ring bed and the collecting section, and the end of the baffle facing the collecting section extends along the second chamber. The end of the guide tube facing the collecting section is located between the partition and the baffle. The product outlet is located at the bottom of the second chamber.

[0013] Preferably, the collecting section further includes a gas phase outlet, which is located between the baffle and the outer ring bed.

[0014] Preferably, the feeding section includes a first mixer, a second mixer, and a liquid distributor, wherein the first mixer and the second mixer are respectively connected to the liquid distributor.

[0015] Preferably, the feed section further includes a first hydrogen inlet and a raw material liquid inlet, the first hydrogen inlet and the raw material liquid inlet being respectively connected to the first mixer.

[0016] Preferably, the feed section further includes a second hydrogen inlet and a liquid circulation inlet, the second hydrogen inlet and the liquid circulation inlet being respectively connected to the second mixer; the liquid circulation inlet is connected to the liquid circulation outlet.

[0017] Secondly, the present invention also provides a hydrogenation method, comprising the self-heating hydrogenation reactor described above, wherein the steps are as follows:

[0018] S1: The hydrogenated feed liquid enters the first mixer through the feed liquid inlet, and hydrogen gas enters the first mixer through the first hydrogen gas inlet. After the hydrogen gas dissolves in the feed liquid, it is transported to the core bed by the liquid distributor and reacts with the catalyst in the core bed under heating.

[0019] S2: After the raw material liquid is heated and reacted to form a circulating liquid, it flows into the first chamber through the guide tube and is transported to the second mixer through the liquid circulation inlet. The hydrogen enters the second mixer through the second hydrogen inlet. After the hydrogen reacts with the circulating liquid for a second time, it enters the outer ring bed through the liquid distributor.

[0020] S3: After the circulating liquid reacts with the catalyst in the outer ring bed, the circulating liquid enters the second chamber along the baffle and is output along the product outlet.

[0021] The embodiments of the present invention bring the following beneficial effects: The shell includes a reaction section and a collection section, and the reaction section includes an outer ring bed and a core bed. Since both the interior of the core bed and the interior of the outer ring bed are filled with catalyst, and the outer ring bed is arranged around the periphery of the core bed, the collection section includes a first chamber and a second chamber. The first chamber is connected to the outer ring bed, and the second chamber is connected to the core bed. During use, the feed liquid first passes through the core bed and reacts once with the catalyst in the core bed. Then, it flows into the outer ring bed through the liquid circulation outlet of the first chamber and undergoes a secondary reaction with the catalyst in the outer ring bed. In this process, the feed temperature and the ratio of hydrogen to raw materials can be controlled in the feeding section to achieve different temperatures for the outer ring bed and the inner core bed. That is, the circulating liquid in the outer ring bed acts as a cold source, and the raw material liquid in the inner core bed can act as a heat source. By relying on the heat of hydrogenation reaction inside the outer ring bed and the inner core bed, the overall temperature required by the equipment can be controlled, so that the hydrogen injected into the reactor can be fully utilized. This alleviates the technical problem in the existing technology where a large amount of hydrogen injected into the reactor does not directly participate in the reaction but is used for cooling, which increases the hydrogen consumption of the reaction and the investment in hydrogen compressors, thus reducing the operating cost. Attached Figure Description

[0022] To more clearly illustrate the specific embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the specific embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present invention. For those skilled in the art, other drawings can be obtained from these drawings without creative effort.

[0023] Figure 1 This is a schematic diagram of the internal structure of a hydrogenation reactor provided in an embodiment of the present invention.

[0024] Reference numerals: 100-Shell; 110-Feed section; 111-First mixer; 112-Second mixer; 113-Liquid distributor; 114-First hydrogen inlet; 115-Raw material inlet; 116-Second hydrogen inlet; 117-Liquid circulation inlet; 120-Reaction section; 121-Outer ring bed; 122-Core bed; 130-Collection section; 131-Baffle; 132-First chamber; 133-Second chamber; 134-Baffle; 135-Liquid circulation outlet; 136-Guide tube; 137-Product outlet; 138-Gas phase outlet. Detailed Implementation

[0025] The technical solution of the present invention will now be clearly and completely described with reference to the accompanying drawings. Obviously, the described embodiments are only some, not all, of the embodiments of the present invention. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.

[0026] In the description of this invention, it should be noted that the terms "horizontal," "inner," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limiting this invention.

[0027] In the description of this invention, it should be noted that, unless otherwise explicitly specified and limited, the term "connected" should be interpreted broadly. For example, it can refer to a fixed connection, a detachable connection, or an integral connection; it can refer to a mechanical connection or an electrical connection; it can refer to a direct connection or an indirect connection through an intermediate medium; and it can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this invention based on the specific circumstances.

[0028] Example 1

[0029] like Figure 1 As shown, this embodiment provides a self-heating hydrogenation reactor, including a shell 100. The shell 100 includes a feed section 110, a reaction section 120, and a collection section 130. The reaction section 120 includes an outer ring bed 121 and an inner ring bed 122. Both the interior of the inner ring bed 122 and the interior of the outer ring bed 121 are filled with catalyst, and the outer ring bed 121 is arranged around the periphery of the inner ring bed 122. The collection section 130 includes a first chamber 132 and a second chamber 133. The first chamber 132 is connected to the inner ring bed 122, and the second chamber 133 is connected to the outer ring bed 121. The first chamber 132 is provided with a liquid circulation outlet 135, which is connected to the outer ring bed 121.

[0030] The housing 100 also includes a feeding section 110, which is located on the upper part of the housing 100, and a reaction section 120 is connected between the feeding section 110 and the collecting section 130.

[0031] The shell 100 includes a reaction section 120 and a collection section 130. The reaction section 120 includes an outer ring bed 121 and a core bed 122. Both the interior of the core bed 122 and the interior of the outer ring bed 121 are filled with catalyst, and the outer ring bed 121 surrounds the periphery of the core bed 122. The collection section 130 includes a first chamber 132 and a second chamber 133. The first chamber 132 is connected to the outer ring bed 121, and the second chamber 133 is connected to the core bed 122. During use, the feed liquid first passes through the core bed 122 and reacts once with the catalyst in the core bed 122. Then, it flows into the outer ring bed 121 through the liquid circulation outlet 135 of the first chamber 132 and reacts with the catalyst. The catalyst in the outer ring bed 121 undergoes a secondary reaction. During this process, the feed temperature and the ratio of hydrogen to raw materials can be controlled in the feed section 110 to achieve different temperatures for the outer ring bed 121 and the inner ring bed 122. That is, the circulating liquid in the outer ring bed 121 acts as a cold source, and the raw material liquid in the inner ring bed 122 can act as a heat source. By relying on the heat of hydrogenation reaction inside the outer ring bed 121 and the inner ring bed 122, the overall temperature required by the equipment can be controlled, so that the hydrogen injected into the reactor can be fully utilized. This alleviates the technical problem in the prior art where a large amount of hydrogen injected into the reactor does not directly participate in the reaction but is used for cooling, which increases the hydrogen consumption of the reaction and the investment in hydrogen compressors, thus reducing the operating cost.

[0032] It should be noted that the self-heating hydrogenation reactor provided in this embodiment is suitable for olefin hydrogenation reaction. The reduction temperature in the outer ring bed and the inner core bed can be controlled by controlling the hydrogen content and space velocity of the gas in the feed section. The feed section 110 is located in the upper part of the shell 100, and the reaction section 120 is connected between the feed section 110 and the collection section 130. The raw material liquid of the primary reaction and the circulating liquid of the secondary reaction can enter the collection section 130 along the reaction section 120 by gravity.

[0033] Furthermore, the connecting pipe between the outer ring bed 121 and the inner core bed 122 can be a finned tube, needle tube, or corrugated tube with a concave-convex waveform, so that the flow velocity and pressure of the liquid inside the connecting pipe change periodically during the flow process, thereby further improving the heat transfer coefficient of the connecting pipe and enhancing the heat transfer efficiency between the outer ring bed 121 and the inner core bed 122.

[0034] Furthermore, the bottom of the collecting section 130 is provided with a partition 131, which is used to divide the collecting section 130 into a first chamber 132 and a second chamber 133.

[0035] The partition plate 131 can be fixedly connected to the collection section 130 by means of snap-fit, threaded connection or welding.

[0036] Furthermore, the collecting section 130 also includes a guide tube 136 and a product outlet 137. The guide tube 136 is connected between the core bed 122 and the collecting section 130. The end of the guide tube 136 facing the collecting section 130 extends along the first chamber 132, and the end of the guide tube 136 facing the collecting section 130 is located between the partition 131 and the baffle 134. The liquid circulation outlet 135 is located at the bottom of the first chamber 132.

[0037] The collection section 130 also includes a guide tube 136 and a product outlet 137. The guide tube 136 is connected between the core bed 122 and the collection section 130. Since the end of the guide tube 136 toward the collection section 130 extends along the first chamber 132, after the raw material liquid in the core bed 122 is mixed with hydrogen, after the core bed 122 reacts with the catalyst, it can flow into the first chamber 132 along the direction of the end of the guide tube 136 toward the collection section 130 extending along the first chamber 132. At the same time, the liquid circulation outlet 135 is located at the bottom of the first chamber 132. The raw material liquid can be drawn out from the liquid circulation outlet 135 through a power component such as a circulation pump and enter the outer ring bed 121.

[0038] Furthermore, the collecting section 130 includes a baffle 134 and a product outlet 137. The baffle 134 is located between the outer ring bed 121 and the collecting section 130, and the end of the baffle 134 facing the collecting section 130 extends along the second chamber 133; the product outlet 137 is located at the bottom of the second chamber 133.

[0039] The collecting section 130 includes a baffle 134, which is disposed between the outer ring bed 121 and the collecting section 130. Since the end of the baffle 134 facing the collecting section 130 extends along the second chamber 133, the raw material liquid flowing from the liquid circulation outlet 135 to the outer ring bed 121 reacts with the catalyst and can flow into the second chamber 133 along the extension direction of the second chamber 133 along the end of the baffle 134 facing the collecting section 130. At the same time, the product outlet 137 is disposed at the bottom of the second chamber 133, and the raw material liquid entering the second chamber 133 flows out along the product outlet 137 for subsequent process operations.

[0040] Furthermore, the aggregate section 130 also includes a gas phase outlet 138, which is located between the baffle 134 and the outer ring bed 121.

[0041] The gas phase outlet 138 is connected to the degassing tank, and the gas phase outlet 138 is used to transport unreacted hydrogen and other gases to the degassing tank to improve the utilization rate of hydrogen.

[0042] Furthermore, the feed section 110 includes a first mixer 111, a second mixer 112, and a liquid distributor 113, with the first mixer 111 and the second mixer 112 respectively connected to the liquid distributor 113.

[0043] Furthermore, the feed section 110 also includes a first hydrogen inlet 114 and a raw material liquid inlet 115, which are respectively connected to the first mixer 111.

[0044] Furthermore, the feed section 110 also includes a second hydrogen inlet 116 and a liquid circulation inlet 117, which are respectively connected to the second mixer 112.

[0045] The first mixer 111 and the second mixer 112 enhance the dissolution of hydrogen in the feed liquid, and the liquid distributor 113 ensures the effective distribution and contact of the feed liquid containing dissolved hydrogen as it drips onto the catalyst bed. Simultaneously, the liquid circulation inlet 117 is connected to the liquid circulation outlet 135, used to guide the feed liquid after one reaction in the inner core bed 122 to the outer ring bed 121.

[0046] Comparative Example 1

[0047] This comparative example provides a composite oil hydrotreating apparatus and a composite oil hydrotreating method (patent number CN201910368675.4), the method comprising:

[0048] (a) An olefin-rich composite oil feedstock from outside the boundary, a recycled composite oil from a hydrotreating unit, and fresh hydrogen from outside the boundary are contacted in a hydrotreating reactor to hydrogenate and saturate unsaturated hydrocarbons and remove sulfur and nitrogen impurities through a hydrogenation reaction; wherein the fresh hydrogen from outside the boundary may be mixed with the composite oil feedstock before entering the hydrotreating reactor, or may be directly entered into the hydrotreating reactor, or optionally enter the inlet of the hydrotreating reactor section.

[0049] (b) The discharge from the hydrotreating reactor enters the hydrotreating separator; the top gas of the hydrotreating separator is extracted as hydrotreating tail gas; the bottom discharge of the hydrotreating separator is divided into two streams, one of which is returned by the hydrotreating circulation pump and the hydrotreating circulation cooler and merged with the olefin-rich composite oil feedstock before entering the hydrotreating reactor, and the other stream is extracted as composite oil hydrotreating product or enters the stripping tower system for stripping.

[0050] As described above, the bed of the hydrotreating reactor can be a single section or divided into multiple sections, such as two or three sections. The outlet of the hydrotreating recirculating cooler can be a single line or divided into multiple lines, such as two or three lines. The fresh hydrogen feed line can be a single line or divided into multiple lines. The bed of the hydrotreating reactor is divided into multiple sections. The outlet of the hydrotreating recirculating cooler is divided into multiple lines. One line is merged with the feed line of the olefin-rich composite oil, and the other lines are connected to the inlet of the hydrotreating reactor section. The fresh hydrogen feed line is divided into multiple lines. One line is merged with the feed line of the olefin-rich composite oil and then connected to the inlet of the hydrotreating reactor or directly connected to the inlet of the hydrotreating reactor. The other lines are connected to the inlet of the hydrotreating reactor section. In this case, the output of the hydrotreating recirculating cooler is divided into multiple streams. One stream is merged with the feed line of the olefin-rich composite oil, and the other streams enter the inlet of the hydrotreating reactor section as circulating material. The fresh hydrogen is divided into multiple streams. One stream is merged with the feed line of the olefin-rich composite oil or directly enters the inlet of the hydrotreating reactor, and the other streams enter the inlet of the hydrotreating reactor section as quench hydrogen and / or supplementary hydrogen.

[0051] Application Example 1

[0052] This application example provides a hydrogenation method, including the self-heating hydrogenation reactor described above, the steps of which are as follows:

[0053] S1: The raw material liquid enters the first mixer 111 through the raw material liquid inlet 115, and the hydrogen gas enters the first mixer 111 through the first hydrogen gas inlet 114. After the hydrogen gas dissolves in the raw material liquid, it is transported to the core bed 122 by the liquid distributor 113 and reacts with the catalyst in the core bed 122 by heating.

[0054] S2: After the raw material liquid is heated and reacted to form a circulating liquid, it flows into the first chamber 132 through the guide tube 136 and is then transported to the second mixer 112 through the liquid circulation inlet 117. Hydrogen gas enters the second mixer 112 through the second hydrogen inlet 116. After the hydrogen gas reacts with the circulating liquid a second time,

[0055] The liquid enters the outer ring bed 121 through the liquid distributor 113;

[0056] S3: After the circulating liquid reacts with the catalyst in the outer ring bed 121, the circulating liquid enters the second chamber 133 along the baffle 134 and is output along the product outlet 137.

[0057] By comparing the comparative example and the application example, it can be seen that the comparative example is equipped with a hydrogenation circulation cooler, and its output is divided into multiple streams. Among them, multiple streams of hydrogen are used as quench hydrogen and / or supplementary hydrogen to enter the inlet of the hydrogenation reactor section. In the application example, by coupling the inner core bed 122 and the outer ring bed 121 in series, the required reaction temperature is maintained solely by the heat of hydrogenation reaction, reducing the need for hydrogen cooling equipment and lowering investment costs.

[0058] It should be noted that the properties of the materials and engineering conditions used in the comparative example and application example are exactly the same, and the required product properties are also exactly the same. The following comparison focuses on hydrogen utilization rate and the number of hydrogenation reactors, as shown in Table 1:

[0059] Table 1

[0060]

[0061] As can be seen from Table 1, compared with Comparative Example 1, Application Example 1 reduces the number of reactors by coupling the inner core bed 122 and the outer ring bed 121 into a single shell, which is equivalent to the two hydrogenation reactors in Comparative Example 1 being connected in series. At the same time, Application Example 1 eliminates equipment such as the hydrogenation preheater, hydrogenation aftercooler, and circulating hydrogen compressor, which greatly reduces the investment in the feedstock preheating system and the cold hydrogen circulation system. Furthermore, all the hydrogen in Application Example 1 is used for the hydrogenation reaction, significantly improving the hydrogen utilization rate. Finally, the feedstock does not need to be preheated or circulated cold hydrogen; the heat of the hydrogenation reaction is effectively utilized by relying solely on the heat exchange of the materials in the inner core bed and the outer ring bed, greatly reducing the consumption of steam and circulating water in the unit and reducing the unit's energy consumption.

[0062] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, and not to limit them; although the present invention has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that modifications can still be made to the technical solutions described in the foregoing embodiments, or equivalent substitutions can be made to some or all of the technical features; and these modifications or substitutions do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A self-heating hydrogenation reactor, characterized in that, The device includes a shell (100), which includes a feed section (110), a reaction section (120), and a collection section (130). The reaction section (120) includes an outer ring bed (121) and a core bed (122). The interior of the core bed (122) and the interior of the outer ring bed (121) are both filled with catalyst, and the outer ring bed (121) is arranged around the periphery of the core bed (122). The collecting section (130) includes a first chamber (132) and a second chamber (133). The first chamber (132) is connected to the inner core bed (122), and the second chamber is connected to the outer ring bed (121). The first chamber (132) is provided with a liquid circulation outlet (135), which is connected to the outer ring bed (121). The bottom of the collecting section (130) is provided with a partition (131), which is used to divide the collecting section (130) into the first chamber (132) and the second chamber (133). The collection section (130) further includes a guide tube (136) and a liquid circulation outlet (135). The guide tube (136) is connected between the core bed (122) and the collection section (130). The end of the guide tube (136) facing the collection section (130) extends along the first chamber (132). The liquid circulation outlet (135) is located at the bottom of the first chamber (132); The collecting section (130) further includes a baffle (134) and a product outlet (137). The baffle (134) is disposed between the outer ring bed (121) and the collecting section (130), and the end of the baffle (134) facing the collecting section (130) extends along the second chamber (133); and the end of the guide tube (136) facing the collecting section (130) is located between the partition (131) and the baffle (134). The product outlet (137) is located at the bottom of the second chamber (133); The feeding section (110) is located on the upper part of the housing (100), and the reaction section (120) is connected between the feeding section (110) and the collecting section (130).

2. The self-heating hydrogenation reactor according to claim 1, characterized in that, The outer ring bed (121) is provided with multiple connecting pipes, which are wound around the periphery of the inner ring bed (122); the connecting pipes are corrugated pipes.

3. The self-heating hydrogenation reactor according to claim 1, characterized in that, The collecting section (130) also includes a gas phase outlet (138), which is located between the baffle (134) and the outer ring bed (121).

4. The hydrogenation reactor according to claim 1, characterized in that, The feed section (110) includes a first mixer (111), a second mixer (112) and a liquid distributor (113), wherein the first mixer (111) and the second mixer (112) are respectively connected to the liquid distributor (113).

5. The hydrogenation reactor according to claim 4, characterized in that, The feed section (110) further includes a first hydrogen inlet (114) and a raw material liquid inlet (115), which are respectively connected to the first mixer (111).

6. The hydrogenation reactor according to claim 4, characterized in that, The feed section (110) further includes a second hydrogen inlet (116) and a liquid circulation inlet (117), the second hydrogen inlet (116) and the liquid circulation inlet (117) being connected to the second mixer (112); the liquid circulation inlet (117) is connected to the liquid circulation outlet (135).

7. A hydrogenation method, characterized in that, The hydrogenation reactor comprising any one of claims 1-6, wherein the steps include: S1: The raw material liquid is introduced into the first mixer (111) through the raw material liquid inlet (115), and hydrogen is introduced into the first mixer (111) through the first hydrogen inlet (114). After the hydrogen dissolves in the raw material liquid, it is transported to the core bed (122) by the liquid distributor (113) and reacted with the catalyst in the core bed (122) by heating. S2: After the raw material liquid is heated and reacted to form a circulating liquid, it flows into the first chamber (132) through the guide tube (136) and is transported to the second mixer (112) through the liquid circulation inlet (117). The hydrogen enters the second mixer (112) through the second hydrogen inlet (116). After the hydrogen reacts with the circulating liquid for a second time, it enters the outer ring bed (121) through the liquid distributor (113). S3: After the circulating liquid reacts with the catalyst in the outer ring bed (121), the circulating liquid enters the second chamber (133) along the baffle (134) and is output along the product outlet (137).

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