CN110170281A - A kind of reactor - Google Patents
A kind of reactor Download PDFInfo
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- CN110170281A CN110170281A CN201910371327.2A CN201910371327A CN110170281A CN 110170281 A CN110170281 A CN 110170281A CN 201910371327 A CN201910371327 A CN 201910371327A CN 110170281 A CN110170281 A CN 110170281A
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- 239000003054 catalyst Substances 0.000 claims abstract description 117
- 238000003786 synthesis reaction Methods 0.000 claims description 15
- 230000015572 biosynthetic process Effects 0.000 claims description 13
- 239000002994 raw material Substances 0.000 claims description 10
- 239000000945 filler Substances 0.000 claims description 6
- 230000001502 supplementing effect Effects 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 4
- 239000011148 porous material Substances 0.000 claims description 3
- 238000012546 transfer Methods 0.000 abstract description 22
- 238000006243 chemical reaction Methods 0.000 abstract description 14
- 238000005336 cracking Methods 0.000 abstract description 4
- 125000004122 cyclic group Chemical group 0.000 abstract 1
- 238000001816 cooling Methods 0.000 description 5
- 238000012856 packing Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000003466 welding Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000000919 ceramic Substances 0.000 description 3
- 238000004891 communication Methods 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000007036 catalytic synthesis reaction Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention provides a kind of reactor, which includes: shell and the heat exchange structure for being set to enclosure interior；Wherein, heat exchange structure is cannula structure comprising Multi-layer exchanging heat endless tube, the radial direction along shell are successively arranged；Interval setting forms the first catalyst layer between two layers of heat exchange endless tube of arbitrary neighborhood；The cross section of each heat exchange endless tube is cyclic structure, to fill into heat transferring medium to exchange heat to catalyst.The present invention exchanges heat to the catalyst of enclosure interior by being arranged to the heat exchange structure of multilayer loop nested structure inside housings, exchanged heat by the catalyst between the heat transferring medium heat exchanging endless tube in heat exchange endless tube, the wire type of shell and tube is replaced to exchange heat by the face formula heat exchange of multilayer loop nested structure, increase film-cooled heat, be conducive to the heat that transfer catalyst reaction is released, improve heat exchange efficiency；The problem of sleeved structure Anti-temperature difference performance reduces well the influence thermally expanded to reactor, avoids the occurrence of heat exchange structure weld cracking.
Description
Technical Field
The invention relates to the technical field of chemical catalytic reaction equipment, in particular to a reactor.
Background
At present, for some strong exothermic reactions such as methanol and low-carbon alcohol synthesis, in order to improve the reaction efficiency, reaction heat is usually removed at the same time of the reaction, in some devices at home and abroad, such as a Lurgi shell-and-tube synthesis tower, shell side water is utilized to remove the reaction heat in a reaction tube, but a byproduct steam tower with a catalyst arranged in a tube is in a linear heat exchange manner, the cooling area is small, the heat removal effect is not good, and the catalyst is easy to cause 'over-temperature' and 'flying temperature', so that the reaction efficiency is influenced; meanwhile, the welded joint of the tube array and the reactor is cracked due to the expansion with heat and the contraction with cold of the tube array, which hinders the development of the reactor and further hinders the development of catalytic synthesis chemical industry.
Disclosure of Invention
In view of the above, the invention provides a reactor, and aims to solve the problems that the heat transfer effect is poor and the welding part of a tube array and the reactor is cracked due to the heat transfer of the existing reactor through a tube array heat exchange tube.
The invention proposes a reactor comprising: the heat exchanger comprises a shell and a heat exchange structure arranged in the shell; the heat exchange structure is a sleeve structure and comprises a plurality of layers of heat exchange ring pipes, and each layer of heat exchange ring pipe is sequentially sleeved along the radial direction of the shell; a first catalyst layer is formed between any two adjacent layers of the heat exchange ring pipes at intervals and is used for filling a catalyst; the cross section of each heat exchange ring pipe is of an annular structure and is used for supplementing a heat exchange medium to exchange heat for the catalyst.
Furthermore, in the reactor, a central heat exchange tube is arranged in a hollow area surrounded by the innermost heat exchange ring tube, and a second catalyst layer is formed between the central heat exchange tube and the innermost heat exchange ring tube at intervals and used for filling a catalyst; and the interior of the central heat exchange tube is used for supplementing a cooling medium.
Further, in the reactor, the ratio of the cross-sectional area of the heat exchange layer to the cross-sectional area of the catalyst layer is 1-5; the cross section area of the heat exchange layer is the sum of the cross section areas of the heat exchange ring pipes and the central heat exchange pipe; the catalyst layer cross-sectional area is the sum of the cross-sectional areas of each of the first catalyst layer and the second catalyst layer.
Furthermore, in the reactor, a hollow area surrounded by the inner wall of the heat exchange ring pipe at the innermost side is used as a third catalyst layer for filling a catalyst, and the ratio of the cross section area of the heat exchange layer to the cross section area of the catalyst is 1-5; the cross section area of the heat exchange layer is the sum of the cross section areas of the heat exchange ring pipes; the catalyst cross-sectional area is the sum of the cross-sectional areas of the respective first and third catalyst layers.
Further, the above reactor further comprises: the first collecting structure and the second collecting structure are respectively arranged at two ends of the heat exchange structure, and the first collecting structure and the second collecting structure are communicated with the heat exchange structure and used for inputting and outputting heat exchange media to the heat exchange structure.
Further, in the reactor, the first collecting structure is arranged at the lower end of the heat exchange structure, and an input port is connected to the first collecting structure and used for inputting a heat exchange medium; the second collection structure is arranged at the upper end of the heat exchange structure, and an output port is connected to the second collection structure and used for outputting a heat exchange medium, so that the flow direction of the heat exchange medium is opposite to that of the raw material synthesis gas in the shell.
Further, in the above reactor, the first collecting structure and/or the second collecting structure is a pipe network structure, and includes a plurality of internal casing pipes; and any adjacent heat exchange circular pipes are communicated through a plurality of inner sleeve connecting pipes.
Furthermore, in the reactor, the inner sleeve connecting pipe arranged on the inner periphery of each heat exchange ring pipe and the inner sleeve connecting pipe arranged on the outer periphery of the heat exchange ring pipe are arranged in a staggered manner.
Further, in the reactor, the inner sleeve connecting pipe is distributed in a scattering shape in the circumferential direction of the heat exchange ring pipe.
Further, in the above reactor, the first collecting structure and/or the second collecting structure is a plate-shaped structure with a hollow interior, and is in communication with each of the heat exchange loops.
Further, in the reactor, the plate-shaped structure is provided with sieve holes at the catalyst layer for communicating the catalyst layer with the filler layer arranged at the upper and lower parts in the shell.
Further, in the above reactor, the heat exchange structure is connected to the shell through a support structure.
According to the reactor provided by the invention, the heat exchange structure with the multilayer ring sleeve structure is arranged in the shell to exchange heat for the catalyst in the shell, namely, the heat exchange medium in the heat exchange ring pipe is used for exchanging heat for the catalyst between the heat exchange ring pipes, and the surface type heat exchange with the multilayer ring sleeve structure replaces the tubular line type heat exchange, so that the cooling area is increased, the heat emitted by the reaction of the catalyst is transferred, and the heat exchange efficiency is further improved; meanwhile, the ring sleeve type structure has good temperature difference resistance, is particularly superior to a tube type structure, and can reduce the influence of thermal expansion on the structure of the reactor, thereby avoiding the problem of cracking of the welding line of the heat exchange structure.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of a reactor provided in an embodiment of the present invention;
FIG. 2 is a sectional view of a reactor provided by an embodiment of the present invention;
FIG. 3 is a further cross-sectional view of a reactor according to an embodiment of the present invention;
fig. 4 is a schematic structural diagram of a collection structure in a reactor according to an embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
Referring to fig. 1, a schematic structural diagram of a reactor according to an embodiment of the present invention is shown. As shown, the reactor comprises: the device comprises a shell 1, a heat exchange structure 2, a packing layer 3 and a support structure 4; wherein,
casing 1 is inside hollow structure, and heat transfer structure 2 sets up in casing 1's inside for carry out the heat transfer to the inside catalyst of casing 1, in order to avoid the catalyst to take place "overtemperature" and "temperature runaway" influence reaction efficiency, certainly also can heat it, avoid its temperature lower influence reaction efficiency.
The heat exchange structure 2 is a sleeve structure, and comprises a plurality of layers of heat exchange ring pipes 21, the diameters of the heat exchange ring pipes 21 are different, and the sleeve structure is used for sequentially sleeving the heat exchange structure in the casing 1 along the radial direction (the horizontal direction shown in figure 1) of the casing 1 so as to divide the casing 1 into a plurality of layers of ring cylindrical cavities for independently storing a catalyst and a heat exchange medium, and then the heat exchange medium is used for carrying out heat exchange on the catalyst to realize the rapid cooling of the catalyst, thereby avoiding the 'overtemperature' and 'temperature runaway' of the catalyst.
Any two adjacent layers of heat exchange ring pipes 21 are arranged at intervals to form a first catalyst layer 22 for filling the catalyst. Specifically, the diameter difference between each layer of heat exchange loop 21 is greater than a preset value, so as to ensure that a cavity is enclosed between any two adjacent layers of heat exchange loops 21 to form a first catalyst layer 22 for filling a catalyst; preferably, each layer of the heat exchange ring pipe 21 is coaxially arranged with the housing 1, so that each layer of the first catalyst layer 22 is uniformly distributed along the circumferential direction of the housing 1, that is, each layer of the first catalyst layer 22 has an annular structure coaxially arranged with the housing 1, and has the same radial width along the housing 1, so as to ensure uniform distribution of the catalyst. Wherein, but also zero clearance setting can be set up at the interval between outside heat transfer ring pipe 21 and the casing 1 inner wall, and, for "overtemperature" and "temperature runaway" of avoiding the catalyst, need not the packing of catalyst between outside heat transfer ring pipe 21 and the casing 1 inner wall, in order to avoid the heat that the catalyst emitted to exert an influence to casing 1, casing 1 is adjacent with heat transfer ring pipe 21 or can be designed outermost heat transfer ring pipe 21 as the shell body in the design process promptly, this kind of design is about to outmost heat transfer ring pipe 21 externally, be different from the inner loop structure, can be heat transfer jacket isotructure and can independently link to each other with water supply system, do not link to each other with the collection structure of inside heat transfer ring.
The cross section of each heat exchange loop pipe 21 is of an annular structure, that is, a cavity is enclosed between the inner wall and the outer wall of the heat exchange loop pipe 21 to form a heat exchange layer 23 for supplementing a heat exchange medium to exchange heat with the catalyst. Preferably, the first catalyst layer 22 and the heat exchange layer 23 are both coaxial ring structures in the casing 1, and the first catalyst layer 22 and the heat exchange layer 23 are arranged at intervals, that is, the heat exchange layer 23 is arranged between any two first catalyst layers 22 and/or the first catalyst layer 22 is arranged between any two heat exchange layers 23, so as to exchange heat for the catalyst in the first catalyst layer 22 by the heat exchange medium in the heat exchange layer 23, thereby avoiding the "overtemperature" and the "runaway temperature" of the catalyst.
The heat exchanging structure 2 is connected to the housing 1 via a support structure 4. Specifically, the number of the supporting structures 4 may be two, so that the upper end and the lower end of the heat exchange structure 2 are connected with the housing 1 through one supporting structure 4, the connection and the fixation between the heat exchange structure 2 and the housing 1 are realized, and the stability of the heat exchange structure 2 is further ensured. In this embodiment, the structure of each support structure 4 is not limited, and only the heat exchange structure 2 needs to be fixed.
In this embodiment, the heat exchange structure 2, which is arranged in the shell 1 in a multi-layer ring sleeve type structure, exchanges heat with the catalyst in the shell 1, that is, the heat exchange medium in the heat exchange ring pipe 21 exchanges heat with the catalyst between the heat exchange ring pipes 21, and the surface heat exchange in the multi-layer ring sleeve type structure replaces tubular linear heat exchange, so that the cooling area is increased, the heat released by the reaction of the catalyst is transferred, and the heat exchange efficiency is further improved; meanwhile, the ring sleeve type structure has good temperature difference resistance, is particularly superior to a tube type structure, and can reduce the influence of thermal expansion on the structure of the reactor, thereby avoiding the problem of cracking of the welding line of the heat exchange structure.
In the above embodiment, the casing body 11 of the casing 1 may be a cylindrical casing with an internal hollow and two open ends, the top of the casing body 11 is detachably connected with the upper end enclosure 12, the bottom of the casing body 11 is detachably connected with the lower end enclosure 13, and preferably, both the upper end enclosure 12 and the lower end enclosure 13 may be detachably connected with the casing body 11 through flanges. The top of the upper end enclosure 12 is provided with an air inlet 121, which is a raw material inlet of the device and is used for inputting raw material synthesis gas into the shell 1. The lower end enclosure 13 is provided with a discharge port 131 which is an outlet for the raw gas to react in the shell 1 to synthesize the product, so that the synthesized product is output. Wherein, the upper end enclosure 12 and/or the lower end enclosure 13 can be provided with a population opening, a discharge opening and the like according to the actual situation so as to facilitate the loading and unloading of the catalyst and the maintenance and the use of equipment. In order to facilitate the uniformity of the distribution of the synthesis gas, it is preferable that the upper part of the shell 1, i.e. the upper head 12, is provided with a packing layer 3 for dispersing the raw synthesis gas so that the synthesis gas is uniformly distributed in each catalyst layer. In order to support the catalyst in the shell 1, a filler layer 3 may be disposed in the lower end enclosure 13 of the shell 1 to support the catalyst and filter the synthesized product. The filler layer 3 is filled with a filler, which can be a ceramic ball or a ceramic ring filler, preferably a ceramic ball.
Referring to fig. 2, which is a cross-sectional view of the reactor provided in the embodiment of the present invention, in the above embodiment, for the first embodiment of the innermost heat exchange loop 21, a central heat exchange tube 24 is disposed in a hollow region surrounded by the innermost heat exchange loop 21, and is spaced apart from the innermost heat exchange loop 21 to form a second catalyst layer 25 for filling with a catalyst, and the central heat exchange tube 24 also serves as a heat exchange layer 23 for supplementing a cooling medium for heat exchange with the catalyst. Specifically, the hollow area refers to a side of the inner wall of the innermost heat exchange ring pipe 21 away from the outer wall of the innermost heat exchange ring pipe 21, that is, the hollow area of the axis position of the ring structure, and may be provided with a central heat exchange tube 24, the central heat exchange tube 24 may be coaxially disposed with the innermost heat exchange ring pipe 21 and spaced apart from the innermost heat exchange ring pipe 21, so as to form a second catalyst layer 25 by enclosing a cavity between the central heat exchange tube 24 and the inner wall of the innermost heat exchange ring pipe 21, so as to fill a catalyst, and the catalyst in the second catalyst layer 25 may be subjected to heat exchange by a cooling medium supplemented inside the central heat exchange tube 24 and the innermost heat exchange ring.
Referring to fig. 3, which is a further cross-sectional view of the reactor provided in the example of the present invention, in the second embodiment of the innermost heat exchange loop 21, a hollow area surrounded by the inner wall of the innermost heat exchange loop 21 is used as a third catalyst layer 26 for packing the catalyst. In particular, the hollow area refers to the side of the inner wall of the innermost heat exchange loop 21 away from the outer wall of the innermost heat exchange loop 21, i.e. the hollow area at the axis position of the ring structure, inside which the catalyst is packed.
In the two embodiments, a central heat exchange tube 24 is disposed at the central position of the innermost heat exchange loop 21 to supplement a heat exchange medium, and a second catalyst layer 25 is formed between the innermost heat exchange loop 21 and the central heat exchange tube 24 at intervals to fill a catalyst; alternatively, the center of the innermost heat exchange loop 21 is directly used as the third catalyst layer 26 for filling the catalyst, i.e. the cross-sections of the heat exchange loop 21, the first catalyst layer 22, the heat exchange layer 23, the second catalyst layer 25 and the third catalyst layer 26 are all ring-shaped structures. No matter how the inside of the innermost heat exchange ring pipe 21 is arranged, in order to ensure that the heat of the catalyst in the synthesis reaction process can be taken out of the reactor by the heat exchange medium in the heat exchange structure 2, preferably, the ratio of the cross section area of the heat exchange layer to the cross section area of the catalyst layer is 1-5, namely, the ratio of the sum of the cross section areas of the heat exchange medium filled in the shell 1 to the sum of the cross section areas of the catalyst filled in the shell 1 is 1: 1-5: 1, so as to ensure that the heat of the catalyst in the synthesis reaction process can be taken out of the reactor by the medium in the heat exchange ring pipe 21, thereby avoiding the overtemperature and runaway temperature of the catalyst and further improving the reaction. Wherein, when the structure in the innermost heat exchange ring pipe 21 is the first embodiment, the cross-sectional area of the heat exchange layer is the sum of the cross-sectional areas of each heat exchange ring pipe 21 and the central heat exchange pipe 24, and the cross-sectional area of the catalyst layer is the sum of the cross-sectional areas of each first catalyst layer 22 and the second catalyst layer 25; for the second embodiment of the configuration in the innermost heat exchange loop 21, the heat exchange layer cross-sectional area is the sum of the cross-sectional areas of the heat exchange loops 21 and the catalyst cross-sectional area is the sum of the cross-sectional areas of the first catalyst layer 22 and the third catalyst layer 26. Wherein, the cross-sectional area of the heat exchange ring pipe 21 is the area of the cavity enclosed between the inner wall and the outer wall on the cross-section of the heat exchange ring pipe 21.
In the above embodiments, the reactor further comprises a first collecting structure 5 and a second collecting structure 6; wherein,
the first collecting structure 5 and the second collecting structure 6 are respectively arranged at two ends of the heat exchanging structure 2 and used for collecting heat exchanging media so as to input and output the heat exchanging media to the heat exchanging structure 2. Wherein, first collection structure 5 is linked together with heat transfer structure 2, and, second collection structure 6 is linked together with heat transfer structure 2, be used for carrying out heat transfer medium's input and output to heat transfer structure 2, certainly, when being equipped with central heat exchange tube 24 to heat transfer ring pipe 21 inside promptly to when the structure is first embodiment in the heat transfer ring pipe 21 of the most inboard, first collection structure 5 and second collection structure 6 all communicate with heat transfer ring pipe 21 and central heat exchange tube 24 homogeneous phase, be used for carrying out heat transfer medium's input and output to heat transfer ring pipe 21 and central heat exchange tube 24. In order to improve the heat exchange effect and efficiency of the heat exchange medium for the catalyst, preferably, the first collecting structure 5 is disposed at the lower end of the heat exchange structure 2, and an input port 51 is connected to the first collecting structure 5 for inputting the heat exchange medium, the second collecting structure 6 is disposed at the upper end of the heat exchange structure 2, and an output port 61 is connected to the second collecting structure 6 for outputting the heat exchange medium, so that the heat exchange medium and the raw syngas in the casing 1 flow in opposite directions, that is, the heat exchange medium is input through the input port 51 and is guided to each layer of heat exchange ring pipe 21 through the first collecting structure 5, and when the structure in the innermost heat exchange ring pipe 21 is the first embodiment, the heat exchange medium is guided to the central heat exchange pipe 24 while being guided to each layer of heat exchange ring pipe 21 through the first collecting structure 5, so that the heat exchange medium flows from bottom to top along the heat exchange ring 21 and the central heat exchange pipe 24 (relative to the position shown in fig. 1) Put another way), the raw material synthesis gas in the shell 1 flows from top to bottom, so that the flow directions of the raw material synthesis gas and the heat exchange medium are opposite, and the countercurrent heat exchange between the raw material synthesis gas and the heat exchange medium is realized, the heat exchange medium in the heat exchange ring pipe 21 and the central heat exchange pipe 24 flows to the upper end and is collected in the second collection structure 6, and the medium after heat exchange of the heat exchange medium is output through the output port 61, for example, steam and water.
In the above embodiments, one embodiment of the first collecting structure 5 and the second collecting structure 6 is a tube-plate structure, and referring to fig. 1 to 2, the first collecting structure 5 and/or the second collecting structure 6 is a plate-shaped structure with a hollow interior, and is communicated with the heat exchanging structure 2, that is, the first collecting structure 5 and/or the second collecting structure 6 is a box-type structure; of course, for the first embodiment of the structure inside the innermost heat exchange loop 21, the first collecting structure 5 and/or the second collecting structure 6 are in communication with both the heat exchange loop 21 and the central heat exchange tube 24. The first collecting structure 5 and/or the second collecting structure 6 are a unitary structure, i.e. a plane where the catalyst layers and the heat exchange layer 23 are connected together, wherein the first collecting structure may be a support plate and the second collecting structure 6 may be a distribution plate.
Referring to fig. 4, it is a schematic structural diagram of a collection structure in a reactor according to an embodiment of the present invention. As shown in the figure, in order to realize the communication between the raw material synthesis gas and the synthesis product, preferably, the plate-shaped structure, i.e. the first collecting structure 5 and/or the second collecting structure 6, is provided with a sieve pore 7 at the catalytic layer for communicating the catalytic layer with the packing layer 3 arranged on the upper and lower parts of the shell 1, so as to ensure the raw material gas in the catalyst to enter and exit, and the sieve pore plays an effective role in distributing the raw material gas. The sieve holes are only arranged at the catalyst layer, that is, the cavity position where the catalyst is arranged, and are not arranged at the heat exchange layer 23. Preferably, the proportion of the screen holes 7 in the plate-shaped structure is 20% to 80%.
The catalyst layer refers to a position to be filled with a catalyst, such as the first catalyst layer 22 and the second catalyst layer 25 in the first embodiment, and the first catalyst layer 22 and the third catalyst layer 26 in the second embodiment.
In the above embodiments, another embodiment of the first collecting structure 5 and the second collecting structure 6 is a pipe-grid structure, see fig. 3, and the first collecting structure 5 and/or the second collecting structure 6 is a pipe-grid structure comprising a plurality of inner casing pipes 8; wherein,
any adjacent heat exchange circular pipes 21 are communicated through a plurality of inner sleeve connecting pipes 8. Specifically, when the structure inside the innermost heat exchange ring pipe 21 is the first embodiment, any adjacent heat exchange ring pipes 21 are communicated through the plurality of inner sleeve connecting pipes 8, and the innermost heat exchange ring pipe 21 and the central heat exchange pipe 24 are also communicated through the plurality of inner sleeve connecting pipes 8, so as to realize the conduction of heat exchange media between the heat exchange pipes. In order to improve the heat exchange effect of the heat exchange medium, the inner sleeve connecting pipe 8 is preferably distributed in a scattering shape in the circumferential direction of the heat exchange circular pipe 21 to avoid local overheating of the catalyst; further preferably, the inner housing tubes 8 are circumferentially equally spaced. Wherein, the inner sleeve pipe 8 can be arranged along the radial direction of the heat exchange ring pipe 21. In order to improve the strength of the heat exchange loop 21 and the stability of the flow of the heat exchange medium in the heat exchange loop 21, it is preferable that the inner sleeve connecting pipe 8 arranged on the inner periphery of each heat exchange loop 21 and the inner sleeve connecting pipe 8 arranged on the outer periphery of the heat exchange loop 21 are arranged in a staggered manner, i.e. the inner sleeve connecting pipe 8 arranged on the inner periphery of each heat exchange loop 21 and the inner sleeve connecting pipe 8 arranged on the outer periphery of the heat exchange loop 21 are not in the same diameter direction of the heat exchange loop 21. In order to reduce the resistance of the heat exchange medium in the inner sleeve union pipe 8, it is preferable that a transition arc is provided at the junction between the inner sleeve union pipe and the heat exchange ring pipe 21, i.e. smooth processing is performed, and certainly, a transition arc is also provided at the junction between the central heat exchange pipe 24 and the inner sleeve union pipe 8.
In summary, in the reactor provided in this embodiment, the heat exchange structure 2 arranged in the shell 1 in the multi-layer ring-shaped structure exchanges heat with the catalyst in the shell 1, that is, the heat exchange medium in the heat exchange loop 21 exchanges heat with the catalyst between the heat exchange loops 21, and the surface heat exchange in the multi-layer ring-shaped structure replaces the tubular linear heat exchange, so as to increase the cooling area, facilitate the transfer of heat released by the catalyst reaction, and further improve the heat exchange efficiency; meanwhile, the ring sleeve type structure has good temperature difference resistance, is particularly superior to a tube type structure, and can reduce the influence of thermal expansion on the structure of the reactor, thereby avoiding the problem of cracking of the welding line of the heat exchange structure.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (12)
1. A reactor, comprising: the heat exchanger comprises a shell (1) and a heat exchange structure (2) arranged inside the shell (1); wherein,
the heat exchange structure (2) is a sleeve structure and comprises a plurality of layers of heat exchange ring pipes (21), and each layer of heat exchange ring pipe (21) is sequentially sleeved along the radial direction of the shell (1);
a first catalyst layer (22) is formed between any two adjacent heat exchange circular pipes (21) at intervals and is used for filling a catalyst;
the cross section of each heat exchange ring pipe (21) is of an annular structure and is used for supplementing a heat exchange medium to exchange heat for the catalyst.
2. The reactor according to claim 1,
a central heat exchange tube (24) is arranged in a hollow area surrounded by the heat exchange ring tube (21) at the innermost side, and a second catalyst layer (25) is formed between the central heat exchange tube and the heat exchange ring tube (21) at intervals and is used for filling a catalyst;
the central heat exchange tube (24) is internally supplemented with a cooling medium.
3. The reactor according to claim 2,
the ratio of the cross-sectional area of the heat exchange layer to the cross-sectional area of the catalyst layer is 1-5; the cross section area of the heat exchange layer is the sum of the cross section areas of the heat exchange ring pipes (21) and the central heat exchange pipe (24); the catalyst layer cross-sectional area is the sum of the cross-sectional areas of the first catalyst layer (22) and the second catalyst layer (25).
4. The reactor according to claim 1,
a hollow area surrounded by the inner wall of the heat exchange ring pipe (21) at the innermost side is used as a third catalyst layer (26) for filling a catalyst, and the ratio of the cross section area of the heat exchange layer to the cross section area of the catalyst is 1-5; the cross section area of the heat exchange layer is the sum of the cross section areas of the heat exchange circular pipes (21); the catalyst cross-sectional area is the sum of the cross-sectional areas of each of the first catalyst layer (22) and the third catalyst layer (26).
5. The reactor of any one of claims 1 to 4, further comprising:
the heat exchange structure comprises a first collecting structure (5) and a second collecting structure (6) which are arranged at two ends of the heat exchange structure (2) respectively, wherein the first collecting structure (5) and the second collecting structure (6) are communicated with the heat exchange structure (2) and used for inputting and outputting heat exchange media to the heat exchange structure (2).
6. The reactor according to claim 5,
the first collecting structure (5) is arranged at the lower end of the heat exchange structure (2), and an input port (51) is connected to the first collecting structure (5) and used for inputting a heat exchange medium;
the second collecting structure (6) is arranged at the upper end of the heat exchange structure (2), and an output port (61) is connected to the second collecting structure (6) and used for outputting a heat exchange medium, so that the flow direction of the heat exchange medium is opposite to that of the raw material synthesis gas in the shell (1).
7. The reactor according to claim 5,
the first collecting structure (5) and/or the second collecting structure (6) are/is a pipe network type structure which comprises a plurality of inner sleeve pipes (8); wherein,
any adjacent heat exchange circular pipes (21) are communicated through a plurality of inner sleeve connecting pipes (8).
8. The reactor according to claim 7,
the inner sleeve connecting pipe (8) arranged on the inner periphery of each heat exchange ring pipe (21) and the inner sleeve connecting pipe (8) arranged on the outer periphery of the heat exchange ring pipe (21) are arranged in a staggered mode.
9. A reactor according to claim 7, characterized in that the inner casing tubes (8) are distributed radially in the circumferential direction of the heat exchange loop (21).
10. The reactor according to claim 5,
the first collecting structure (5) and/or the second collecting structure (6) is/are a plate-like structure with a hollow interior, and is communicated with each heat exchange loop (21).
11. The reactor of claim 10,
the plate-shaped structure is provided with sieve pores (7) at the catalyst layer for communicating the catalyst layer with the filler layers (3) arranged at the upper part and the lower part in the shell (1).
12. A reactor according to any of claims 1 to 4, characterized in that the heat exchange structure (2) is connected to the shell (1) by means of a support structure (4).
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| CN201910371327.2A CN110170281A (en) | 2019-05-06 | 2019-05-06 | A kind of reactor |
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| CN201910371327.2A CN110170281A (en) | 2019-05-06 | 2019-05-06 | A kind of reactor |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111735068A (en) * | 2020-06-10 | 2020-10-02 | 苏州华烯环保科技有限公司 | Waste gas catalytic combustion device |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3127247A (en) * | 1964-03-31 | Alternate annular isothermal reactor | ||
| CN1941485A (en) * | 2005-09-27 | 2007-04-04 | 三星Sdi株式会社 | Fuel reforming apparatus |
| CN107224940A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of methanator and methanation process |
-
2019
- 2019-05-06 CN CN201910371327.2A patent/CN110170281A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3127247A (en) * | 1964-03-31 | Alternate annular isothermal reactor | ||
| CN1941485A (en) * | 2005-09-27 | 2007-04-04 | 三星Sdi株式会社 | Fuel reforming apparatus |
| CN107224940A (en) * | 2016-03-23 | 2017-10-03 | 中国石化工程建设有限公司 | A kind of methanator and methanation process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111735068A (en) * | 2020-06-10 | 2020-10-02 | 苏州华烯环保科技有限公司 | Waste gas catalytic combustion device |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
| CN112044363B (en) * | 2020-08-31 | 2022-09-13 | 江苏永大化工机械股份有限公司 | Coupling reactor for producing ethylene glycol from coal |
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