Composite reactor

Abstract

The invention relates to the field of reactors, and discloses a composite reactor which comprises a shell, an upper sealing head arranged at the upper end of the shell and a lower sealing head arranged at the lower end of the shell, and reaction gas inlets coaxial with the shell are formed in the upper sealing head and the lower sealing head respectively. The shell is internally provided with a catalyst bed layer and two gas distribution pipes which respectively extend towards the catalyst bed layer from the two reaction gas inlets along the axial direction of the shell, an axial interval is formed between the tail ends of the two gas distribution pipes, a plurality of gas distribution holes are uniformly distributed in the pipe walls, extending into the catalyst bed layer, of the gas distribution pipes, and a reaction gas outlet is formed in the middle of the shell. According to the composite reactor, a reaction gas inlet and a gas distribution pipe are respectively arranged at two axial ends of the reactor, and a reaction gas outlet is formed in the middle of the reactor, so that reaction gas flows both radially and axially when passing through a catalyst bed layer, the flow resistance is reduced, the passing distance of the reaction gas and the sectional area of a flow channel are large, and the reaction gas flow is uniform. The reaction volume is fully utilized, the structure is simple and reliable, and large-scale production is facilitated.

Description

Technical Field

[0001] The invention relates to the field of reactors, in particular to a composite reactor. Background Art

[0002] Reactors are equipment that realize reaction processes and are widely used in petrochemicals, coal chemicals, oil refining, metallurgy and other fields. They are most mature in continuous reforming, coal chemicals, methanol to olefins and other processes. In the reactor, a large number of solid particles are piled together to form a particle bed with a certain height. These solid particles can be reactants or catalysts. Reactors can be divided into fixed bed reactors, fluidized bed reactors and slurry bed reactors according to the shape of the solid particle bed.

[0003] Among them, fixed bed reactors are the most widely used in industry because of their small catalyst mechanical wear, the flow of fluid in the bed is close to plug flow, a smaller amount of catalyst and a smaller reactor volume can be used to obtain a larger production capacity, controllable residence time and adjustable temperature distribution are conducive to high selectivity and conversion rate, and can be operated at high temperature and high pressure. Fixed bed reactors can be divided into adiabatic reactors and heat exchange reactors according to the heat transfer method, and can be divided into axial reactors and radial reactors according to the flow direction of the reaction gas.

[0004] Among them, the most common heat exchange reactor is the tube-type fixed bed reactor. In the axial tube-type reactor, the tube side is the reaction gas with relatively high pressure, the catalyst is loaded in the tube, the reaction gas flows axially through the catalyst tube, and the shell side is the cold material with relatively low pressure. The heat released by the reaction is transferred to the cold material outside the tube through the tube wall; the advantages are that the catalyst is easy to load and unload, the specific cold area is large, and the "time and space yield" of the catalyst is high; the disadvantages are that the axial flow resistance of the reaction gas is large, the catalyst particle size is large, the heat exchange tube requires duplex steel, the welding is difficult and the manufacturing cost is high, and the shell manufacturing is limited after large-scale. In a radial tube reactor, the tube side is cold material with relatively low pressure, the shell side is reaction gas with relatively high pressure, the catalyst is loaded between the tubes, the reaction gas flows radially through the catalyst bed, and the heat released by the reaction is transferred to the cold material in the tube through the tube wall; the advantages are that the radial flow resistance of the reaction gas is small, the production scale can be increased by increasing the height while the reactor diameter remains unchanged, the catalyst bed temperature is uniform and adjustable, there are few side reactions, the product quality is high, the requirements for heat exchange tube materials are relatively low, and the manufacturing cost is low; the disadvantages are that the heat transfer area is small and a large number of cold tubes are required. Summary of the invention

[0005] The object of the present invention is to provide a composite reactor which can combine the advantages of an axial tube-in-tube reactor and a radial tube-in-tube reactor.

[0006] In order to achieve the above-mentioned purpose, the present invention provides a composite reactor, comprising a shell, an upper head arranged at the upper end of the shell and a lower head arranged at the lower end of the shell, the upper head and the lower head are respectively provided with reaction gas inlets, the reaction gas inlets are coaxial with the shell, a catalyst bed and two gas distribution pipes extending from the two reaction gas inlets along the axial direction of the shell toward the catalyst bed are respectively provided in the shell, there is an axial spacing between the ends of the two gas distribution pipes, a plurality of gas distribution holes are evenly distributed on the tube wall of the gas distribution pipe extending into the catalyst bed, and a reaction gas outlet is provided in the middle of the shell.

[0007] Optionally, the air distribution holes located on the peripheral wall of the air distribution pipe are axially arranged to extend along the radial direction of the air distribution pipe or to extend obliquely relative to the radial direction toward the reaction gas outlet; the air distribution holes located on the end wall of the air distribution pipe are axially arranged to extend along the axial direction of the air distribution pipe or to extend obliquely relative to the axial direction toward the reaction gas outlet.

[0008] Optionally, a catalyst inlet is provided on the upper head, and a catalyst outlet is provided on the lower head.

[0009] Optionally, a section of the tube wall of the gas distribution tube adjacent to the catalyst bed is not provided with the gas distribution holes to form an insulating section.

[0010] Optionally, a gas collector is provided in the shell, and the gas collector is connected between the catalyst bed and the reaction gas outlet.

[0011] Optionally, the gas collector includes a collecting tube coaxially sleeved in the shell, both ends of the collecting tube are respectively connected to the shell, an outer wall surface of the collecting tube and an inner wall surface of the shell are radially spaced to form a gas collecting chamber, the reaction gas outlet is connected to the gas collecting chamber, and a plurality of gas collecting holes connected to the gas collecting chamber are evenly distributed on the wall of the collecting tube.

[0012] Optionally, the axial length of the collecting cylinder is less than or equal to the axial length of the catalyst bed.

[0013] Optionally, two pipe box assemblies and a plurality of heat exchange tubes are provided in the shell, the two pipe box assemblies are respectively located above and below the catalyst bed, the plurality of heat exchange tubes extend along the axial direction of the shell and are arranged in the catalyst bed at intervals along the radial direction of the shell, the upper and lower ends of the heat exchange tubes are respectively connected to the two pipe box assemblies, the upper head is provided with a heat exchange medium outlet connected to the upper pipe box assembly, and the lower head is provided with a heat exchange medium inlet connected to the lower pipe box assembly.

[0014] Optionally, the lower pipe-box assembly is fixedly arranged to form a fixed end, and the upper pipe-box assembly is floatingly arranged to form a floating end.

[0015] Optionally, the plurality of heat exchange tubes form multiple layers concentrically arranged around the air distribution pipe, and the pipe box assembly includes a plurality of annular pipe boxes concentrically arranged around the air distribution pipe, and radial spacing is provided between the plurality of annular pipe boxes and between the annular pipe boxes and the air distribution pipe. The plurality of annular pipe boxes correspond one-to-one to the multiple layers of heat exchange tubes, and both ends of each layer of the heat exchange tubes are respectively connected to the tube sheets of the corresponding annular pipe boxes and are connected to the interior of the annular pipe boxes.

[0016] Optionally, the upper head is provided with a plurality of heat exchange medium outlets respectively connected to the plurality of annular pipe boxes above, and the lower head is provided with a plurality of heat exchange medium inlets respectively connected to the plurality of annular pipe boxes below.

[0017] Optionally, both ends of the heat exchange tubes are bent centripetally and then connected to the tube sheet.

[0018] Optionally, the heat exchange medium outlet is communicated with the corresponding annular pipe box through a medium outlet pipe, and an expansion joint is provided on the medium outlet pipe; the heat exchange medium inlet is communicated with the corresponding annular pipe box through a medium inlet pipe.

[0019] Through the above technical scheme, the composite reactor of the present invention respectively arranges a reaction gas inlet and a gas distribution pipe at the axial ends of the reactor, and arranges a reaction gas outlet in the middle of the reactor, so that the reaction gas flows through the catalyst bed with both radial flow and axial flow, the flow resistance is reduced, the reaction gas flows over a large distance and the cross-sectional area of ​​the flow channel, the reaction volume is fully utilized, the structure is simple and reliable, and it is conducive to large-scale.

[0020] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] The accompanying drawings constituting a part of the present invention are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation of the present invention. In the accompanying drawings:

[0022] Figure 1 It is a structural schematic diagram of an embodiment of the composite reactor of the present invention;

[0023] Figure 2 It is a structural schematic diagram of another embodiment of the expansion joint in the present invention.

[0024] Description of Reference Numerals

[0025] 10-shell, 101-reaction gas inlet, 102-reaction gas outlet, 11-upper head, 111-catalyst inlet, 112-medium outlet pipeline, 113-expansion joint, 12-lower head, 121-catalyst outlet, 122-medium inlet pipeline, 13-catalyst bed, 14-gas distribution pipe, 141-insulation section, 15-collecting tube, 151-gas collecting chamber, 16-heat exchange tubes, 17-annular pipe box, 171-tube sheet. DETAILED DESCRIPTION

[0026] The embodiments of the present invention are further described in detail below in conjunction with the accompanying drawings. The detailed description of the following embodiments and the accompanying drawings are used to exemplarily illustrate the principles of the present invention, but cannot be used to limit the scope of the present invention. The present invention can be implemented in many different forms and is not limited to the specific embodiments disclosed herein, but includes all technical solutions within the scope of the claims.

[0027] The present invention provides these embodiments to make the present invention thorough and complete, and fully express the scope of the present invention to those skilled in the art. It should be noted that unless otherwise specifically stated, the relative arrangement of the parts and steps, the composition of the materials, the numerical expressions and the numerical values ​​described in these embodiments should be interpreted as being merely exemplary, rather than as limiting.

[0028] It should be noted that, in the description of the present invention, unless otherwise specified, the meaning of "multiple" is greater than or equal to two; the terms "upper", "lower", "left", "right", "inner", "outer", etc., indicating the orientation or positional relationship, are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as a limitation on the present invention. When the absolute position of the object being described changes, the relative positional relationship may also change accordingly.

[0029] In addition, the words "first", "second" and similar words used in the present invention do not indicate any order, quantity or importance, but are only used to distinguish different parts. "Vertical" is not strictly perpendicular, but is within the tolerance range. "Parallel" is not strictly parallel, but is within the tolerance range. "Include" or "comprising" and similar words mean that the elements before the word include the elements listed after the word, and do not exclude the possibility of including other elements.

[0030] It should also be noted that in the description of the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected" and "connected" should be understood in a broad sense. For example, it can be a fixed connection, a detachable connection, or an integral connection; it can be directly connected or indirectly connected through an intermediate medium. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to the specific circumstances. When a specific device is described as being located between a first device and a second device, there may or may not be an intermediate device between the specific device and the first device or the second device.

[0031] All terms used in the present invention have the same meanings as those understood by ordinary technicians in the field to which the present invention belongs, unless otherwise specifically defined. It should also be understood that terms defined in general dictionaries, such as general dictionaries, should be interpreted as having meanings consistent with their meanings in the context of the relevant technology, and should not be interpreted in an idealized or extremely formal sense, unless explicitly defined herein.

[0032] Technologies, methods, and equipment known to ordinary technicians in the relevant art may not be discussed in detail, but where appropriate, the technologies, methods, and equipment should be considered part of the specification.

[0033] The present invention provides a composite reactor, see Figure 1 , comprising a shell 10, an upper head 11 arranged at the upper end of the shell 10 and a lower head 12 arranged at the lower end of the shell 10, a reaction gas inlet 101 is respectively arranged on the upper head 11 and the lower head 12, the reaction gas inlet 101 is coaxial with the shell 10, a catalyst bed 13 and two gas distribution pipes 14 extending from the two reaction gas inlets 101 along the axial direction of the shell 10 toward the catalyst bed 13 are arranged in the shell 10, there is an axial interval between the ends of the two gas distribution pipes 14, a plurality of gas distribution holes are evenly distributed on the tube wall of the gas distribution pipe 14 extending into the catalyst bed 13, and a reaction gas outlet 102 is arranged in the middle of the shell 10.

[0034] In the above description, it can be understood that the end of the gas distribution pipe 14 close to the reaction gas inlet 101 is an open end, and the end extending into the catalyst bed 13 is a closed end, that is, the terminal in the above description. Preferably, the two gas distribution pipes 14 are symmetrically arranged up and down, and the reaction gas outlet 102 is located in the axial interval between the two gas distribution pipes 14 in the vertical direction.

[0035] During the reaction, the reaction gas enters the gas distribution pipe 14 through the reaction gas inlet 101 , then flows out through the gas distribution holes on the gas distribution pipe 14 , flows through the catalyst bed 13 in radial and axial directions, and finally flows out through the reaction gas outlet 102 .

[0036] The composite reactor of the present invention respectively arranges a reaction gas inlet 101 and a gas distribution pipe 14 at both axial ends of the reactor, and arranges a reaction gas outlet 102 in the middle of the reactor, so that the reaction gas flows through the catalyst bed 13 with both radial flow and axial flow, the flow resistance is reduced, the reaction gas flows over a large distance and the flow channel cross-sectional area, the reaction volume is fully utilized, the structure is simple and reliable, and it is conducive to large-scale.

[0037] In the above, it can be understood that the gas distribution pipe 14 includes a peripheral wall and an end wall located at the end. The axial direction of the gas distribution holes located on the peripheral wall of the gas distribution pipe 14 can be set to extend along the radial direction of the gas distribution pipe 14 or extend obliquely relative to the radial direction toward the reaction gas outlet 102. The axial direction of the gas distribution holes located on the end wall of the gas distribution pipe 14 can be set to extend along the axial direction of the gas distribution pipe 14 or extend obliquely relative to the axial direction toward the reaction gas outlet 102. Among them, by setting the axial direction of the gas distribution holes to extend obliquely toward the reaction gas outlet 102, it is more conducive to reducing the flow resistance drop of the reaction gas.

[0038] like Figure 1 As shown, the upper end cap 11 may be provided with a catalyst inlet 111, and the lower end cap 12 may be provided with a catalyst outlet 121 for loading and unloading the catalyst. The axial directions of the catalyst inlet 111 and the catalyst outlet 121 may be inclined to the axial direction of the reaction gas inlet 101. The catalyst inlet 111 and the catalyst outlet 121 may be located on both sides of the central axis of the reactor, respectively.

[0039] In some embodiments, Figure 1 As shown, a section of the wall of the gas distribution pipe 14 adjacent to the catalyst bed 13 is not provided with gas distribution holes to form an insulating section 141. It can be understood that a portion of the insulating section 141 is located in the catalyst bed, and another portion is located outside the catalyst bed. By providing the insulating section 141, after the feed reaction gas enters the insulating section 141, it can be pre-heated by the heat generated by the exothermic reaction in the catalyst bed, thereby widening the applicable temperature range of the reaction gas.

[0040] In some embodiments, a gas collector is disposed in the housing 10, and the gas collector is connected between the catalyst bed 13 and the reaction gas outlet 102. The provision of the gas collector is conducive to the discharge of the reaction gas.

[0041] Specifically, Figure 1As shown, the gas collector includes a collecting tube 15 coaxially sleeved in the shell 10, and the two ends of the collecting tube 15 are respectively connected to the shell 10. There is a radial interval between the outer wall surface of the collecting tube 15 and the inner wall surface of the shell 10 to form a gas collecting chamber 151. The reaction gas outlet 102 is connected to the gas collecting chamber 151, and a plurality of gas collecting holes connected to the gas collecting chamber 151 are evenly distributed on the cylinder wall of the collecting tube 15. It can be understood that the gas collecting chamber 151 is an annular cavity, and the gas collecting holes can be used for the reaction gas to pass through, and the catalyst particles are prevented from passing through. Among them, the reaction gas outlet 102 can be a plurality of circumferentially spaced intervals along the shell 10. The axial length of the collecting tube 15 is less than or equal to the axial length of the catalyst bed 13. By setting the collecting tube 15, the collecting tube 15 can separate the catalyst bed 13 from the reaction gas outlet 102, prevent the catalyst particles from blocking the reaction gas outlet 102, and facilitate the collection and discharge of the reaction gas.

[0042] Of course, the gas collector of the present invention is not limited to the above-mentioned embodiments. For example, in other embodiments, the gas collector may include a plurality of collection hoods arranged at circumferential intervals along the shell 10, each collection hood corresponding to a reaction gas outlet 102, and the collection hood covers the reaction gas outlet 102 inside the shell, and connects the reaction gas outlet 102 with the catalyst bed 13.

[0043] In the present invention, see Figure 1 Two pipe box assemblies and a plurality of heat exchange tubes 16 are also provided in the shell 10. The two pipe box assemblies are respectively located above and below the catalyst bed 13. The plurality of heat exchange tubes 16 extend along the axial direction of the shell 10 and are arranged in the catalyst bed 13 at intervals along the radial direction of the shell 10. The upper and lower ends of the heat exchange tubes 16 are respectively connected to the two pipe box assemblies. The upper head 11 is provided with a heat exchange medium outlet connected to the upper pipe box assembly, and the lower head 12 is provided with a heat exchange medium inlet connected to the lower pipe box assembly.

[0044] In order to adapt to the expansion and contraction of the heat exchange tubes, the lower tube box assembly is fixedly arranged to form a fixed end, and the upper tube box assembly is floatingly arranged to form a floating end. The tube side of the heat exchange tubes 16 can be a cold material with a relatively low pressure, and the shell side of the shell 10 is a reaction gas with a relatively high pressure. The catalyst is loaded between the heat exchange tubes, and the heat released by the reaction is transferred to the cold material in the tube through the tube wall of the heat exchange tubes 16. When the cold material is boiler water, medium-pressure steam can be produced as a by-product, and energy utilization is reasonable. In other words, boiler water can enter the heat exchange tubes 16 through the heat exchange medium inlet, and the generated steam is discharged from the heat exchange medium inlet.

[0045] In some embodiments, Figure 1As shown, a plurality of heat exchange tubes 16 form multiple layers arranged concentrically around the gas distribution pipe 14, and the pipe box assembly includes a plurality of annular pipe boxes 17 arranged concentrically around the gas distribution pipe 14, and radial intervals are provided between the plurality of annular pipe boxes 17 and between the annular pipe boxes and the gas distribution pipe 14, and the plurality of annular pipe boxes 17 correspond one to one with the multiple layers of heat exchange tubes 16, and both ends of each layer of heat exchange tubes 16 are respectively connected to the tube sheet 171 of the corresponding annular pipe box 17, and communicate with the interior of the annular pipe box 17. By such an arrangement, the loading and unloading of the catalyst can be facilitated, and the heat exchange tubes 16 are evenly distributed throughout the catalyst bed 13, and the heat transfer area is large with a large number of pipes.

[0046] Preferably, the upper end cap 11 is provided with multiple heat exchange medium outlets respectively connected to the multiple annular pipe boxes 17 above, and the lower end cap 12 is provided with multiple heat exchange medium inlets respectively connected to the multiple annular pipe boxes 17 below. Through the above arrangement, the heat exchange medium in the tube pass of the heat exchange tubes 16 can be matched with different materials according to the heat exchange needs, that is, the heat exchange medium in the tube pass of the heat exchange tubes 16 of different layers can be the same or different. Of course, in other embodiments, there may be only one heat exchange medium outlet and one heat exchange medium inlet, in which case the multiple annular pipe boxes 17 are interconnected, and the heat exchange medium is the same.

[0047] Among them, Figure 1 As shown, the two ends of the heat exchange tube 16 are bent centripetally and connected to the tube sheet 171. After the two ends of the heat exchange tube 16 are bent centripetally, the width of the tube sheet 171 can be reduced, which is convenient for welding the heat exchange tube 16 and the tube sheet 171 and for loading and unloading the catalyst.

[0048] like Figure 1 As shown, the heat exchange medium outlet is connected to the corresponding annular pipe box 17 through the medium outlet pipe 112, and an expansion joint 113 is provided on the medium outlet pipe 112; the heat exchange medium inlet is connected to the corresponding annular pipe box 17 through the medium inlet pipe 122. Among them, the expansion joint 113 can be connected to the medium outlet pipe 112 (see Figure 1 ), the expansion joint 113 can also form a sleeve structure with the medium outlet pipe 112 (see Figure 2 ).

[0049] In the present invention, the annular pipe box 17, the heat exchange medium inlet, the heat exchange medium outlet, the reaction gas inlet 101, and the reaction gas outlet 102 are preferably two or more, so that the materials in the tube side and the shell side can be evenly distributed, the inlet and outlet flow rates and pressure drops can be reduced, the speed and pressure of the reaction gas in the catalyst bed can be optimized, the uniformity of the bed temperature distribution can be improved, the reactor conversion rate and product quality can be improved, and energy utilization can be reasonable.

[0050] From the above, the present invention provides a composite reactor with simple and reliable structure, small axial radial flow resistance drop of reaction gas, easy loading and unloading of catalyst, uniform and adjustable catalyst bed temperature, few side reactions, high product quality, reasonable energy utilization, adiabatic isothermal catalyst bed to broaden the applicable temperature range of reaction gas, and easy large-scale operation.

[0051] The composite reactor of the present invention has the advantages of easy catalyst loading and unloading and large heat transfer area of ​​the existing axial shell and tube reactor, and also has the advantages of small flow resistance drop, uniform and adjustable catalyst bed temperature, few side reactions, high product quality and easy large-scale production of the existing radial shell and tube reactor.

[0052] So far, various embodiments of the present invention have been described in detail. In order to avoid obscuring the concept of the present invention, some details known in the art are not described. Based on the above description, those skilled in the art can fully understand how to implement the technical solution disclosed herein.

[0053] Although some specific embodiments of the present invention have been described in detail by way of examples, it should be understood by those skilled in the art that the above examples are for illustration only and are not intended to limit the scope of the present invention. It should be understood by those skilled in the art that the above embodiments may be modified or some technical features may be replaced by equivalents without departing from the scope and spirit of the present invention. In particular, the various technical features mentioned in the various embodiments may be combined in any manner as long as there is no structural conflict.

Claims

1. A composite reactor, characterized in that: The invention comprises a shell (10), an upper end cap (11) arranged at the upper end of the shell (10), and a lower end cap (12) arranged at the lower end of the shell (10), wherein the upper end cap (11) and the lower end cap (12) are respectively provided with a reaction gas inlet (101), and the reaction gas inlet (101) is coaxial with the shell (10), a catalyst bed (13) and two gas distribution pipes (14) extending from the two reaction gas inlets (101) along the axial direction of the shell (10) toward the catalyst bed (13) are provided in the shell (10), an axial spacing is provided between the ends of the two gas distribution pipes (14), a plurality of gas distribution holes are evenly distributed on the tube wall of the gas distribution pipe (14) extending into the catalyst bed (13), and a reaction gas outlet (102) is provided in the middle of the shell (10).

2. The composite reactor according to claim 1, characterized in that: The air distribution holes located on the peripheral wall of the air distribution pipe (14) are axially arranged to extend along the radial direction of the air distribution pipe (14) or to extend obliquely relative to the radial direction toward the reaction gas outlet (102); the air distribution holes located on the end wall of the air distribution pipe (14) are axially arranged to extend along the axial direction of the air distribution pipe (14) or to extend obliquely relative to the axial direction toward the reaction gas outlet (102); and / or The upper end cap (11) is provided with a catalyst inlet (111), and the lower end cap (12) is provided with a catalyst outlet (121).

3. The composite reactor according to claim 1, characterized in that: A section of the wall of the gas distribution pipe (14) adjacent to the catalyst bed (13) is not provided with the gas distribution holes, so as to form a heat-insulating section (141).

4. The composite reactor according to claim 1, characterized in that: A gas collector is arranged in the shell (10), and the gas collector is connected between the catalyst bed (13) and the reaction gas outlet (102).

5. The composite reactor according to claim 4, characterized in that: The gas collector comprises a collecting tube (15) coaxially sleeved in the shell (10), the two ends of the collecting tube (15) being respectively connected to the shell (10), a radial spacing being provided between the outer wall surface of the collecting tube (15) and the inner wall surface of the shell (10) to form a gas collecting chamber (151), the reaction gas outlet (102) being connected to the gas collecting chamber (151), and a plurality of gas collecting holes being evenly distributed on the tube wall of the collecting tube (15) and connected to the gas collecting chamber (151).

6. The composite reactor according to claim 5, characterized in that: The axial length of the collecting cylinder (15) is less than or equal to the axial length of the catalyst bed (13).

7. The composite reactor according to any one of claims 1 to 6, characterized in that: Two pipe box assemblies and a plurality of heat exchange tubes (16) are arranged in the shell (10), the two pipe box assemblies are respectively located above and below the catalyst bed (13), the plurality of heat exchange tubes (16) extend along the axial direction of the shell (10) and are arranged in the catalyst bed (13) at intervals along the radial direction of the shell (10), the upper and lower ends of the heat exchange tubes (16) are respectively connected to the two pipe box assemblies, the upper end cap (11) is provided with a heat exchange medium outlet connected to the upper pipe box assembly, and the lower end cap (12) is provided with a heat exchange medium inlet connected to the lower pipe box assembly.

8. The composite reactor according to claim 7, characterized in that: The lower pipe-box assembly is fixedly arranged to form a fixed end, and the upper pipe-box assembly is floatingly arranged to form a floating end; and / or The plurality of heat exchange tubes (16) form multiple layers concentrically arranged around the air distribution pipe (14); the pipe box assembly comprises multiple annular pipe boxes (17) concentrically arranged around the air distribution pipe (14); radial spacing is provided between the multiple annular pipe boxes (17) and between the annular pipe boxes (17) and the air distribution pipe (14); the multiple annular pipe boxes (17) correspond one-to-one to the multiple layers of heat exchange tubes (16); both ends of each layer of the heat exchange tubes (16) are respectively connected to the tube sheet (171) of the corresponding annular pipe box (17), and are communicated with the interior of the annular pipe box (17).

9. The composite reactor according to claim 8, characterized in that: The upper end cap (11) is provided with a plurality of heat exchange medium outlets respectively connected to the plurality of annular pipe boxes (17) above, and the lower end cap (12) is provided with a plurality of heat exchange medium inlets respectively connected to the plurality of annular pipe boxes (17) below.

10. The composite reactor according to claim 8, characterized in that: The two ends of the heat exchange tubes (16) are bent centripetally and then connected to the tube sheet (171), and / or The heat exchange medium outlet is connected to the corresponding annular pipe box (17) through a medium outlet pipe (112), and an expansion joint (113) is provided on the medium outlet pipe (112); the heat exchange medium inlet is connected to the corresponding annular pipe box (17) through a medium inlet pipe (122).

Images