CN116492938A - Reactor and application thereof - Google Patents
Reactor and application thereof Download PDFInfo
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- CN116492938A CN116492938A CN202310321759.9A CN202310321759A CN116492938A CN 116492938 A CN116492938 A CN 116492938A CN 202310321759 A CN202310321759 A CN 202310321759A CN 116492938 A CN116492938 A CN 116492938A
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- Prior art keywords
- metal
- tube
- shell
- metal tube
- reactor
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- 239000002184 metal Substances 0.000 claims abstract description 319
- 239000000463 material Substances 0.000 claims abstract description 122
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 238000006243 chemical reaction Methods 0.000 claims abstract description 52
- 239000002245 particle Substances 0.000 claims description 27
- 229910052739 hydrogen Inorganic materials 0.000 claims description 13
- 239000001257 hydrogen Substances 0.000 claims description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 12
- 239000011148 porous material Substances 0.000 claims description 9
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 238000000034 method Methods 0.000 claims description 8
- 239000000446 fuel Substances 0.000 claims description 7
- 230000007613 environmental effect Effects 0.000 claims description 5
- 238000005272 metallurgy Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 238000005516 engineering process Methods 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- 238000005859 coupling reaction Methods 0.000 claims description 3
- 238000012546 transfer Methods 0.000 abstract description 10
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 39
- 230000000694 effects Effects 0.000 description 8
- 238000001651 catalytic steam reforming of methanol Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 6
- 238000009834 vaporization Methods 0.000 description 6
- 230000008016 vaporization Effects 0.000 description 6
- 238000009826 distribution Methods 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000003014 reinforcing effect Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000010963 304 stainless steel Substances 0.000 description 3
- 229910000589 SAE 304 stainless steel Inorganic materials 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000007084 catalytic combustion reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 241001391944 Commicarpus scandens Species 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000010431 corundum Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- 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
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00309—Controlling the temperature by indirect heat exchange with two or more reactions in heat exchange with each other, such as an endothermic reaction in heat exchange with an exothermic reaction
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/06—Details of tube reactors containing solid particles
- B01J2208/065—Heating or cooling the reactor
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to a reactor and application thereof. The reactor comprises: a metal housing comprising; the metal tube bundle is arranged in the metal shell; the metal tube bundle comprises metal tubes which are arranged in parallel; two ends of the metal tube are connected to the first surface and the second surface; the metal shell comprises a material inlet and a material outlet; a shell pass is formed between the shell and the outer wall of the metal tube; the inner cavity of the metal tube forms a tube pass; the shell side is filled with a granular first catalyst, and/or the tube side is filled with a granular and/or honeycomb second catalyst; the metal fins are arranged on the outer wall of the metal tube; the metal fins divide the shell pass into sections which are communicated with each other; the first material is output from a material outlet after interval reaction; and/or the second material reacts via tube side; when the reactor is operated, the flow direction of the materials in the metal tube bundle in the shell pass is perpendicular to the length direction of the metal tube. The invention aims to solve the technical problem of providing a reactor which has the advantages of high structural compactness, good heat transfer and mass transfer performance and low cost.
Description
Technical Field
The invention belongs to the technical fields of chemistry, chemical metallurgy, environmental protection and hydrogen energy and fuel cells, and particularly relates to a reactor and application thereof.
Background
In the technical fields of chemistry, chemical metallurgy, environmental protection and hydrogen energy and fuel cells, the structure of a reactor adopted in the process of carrying out chemical reactions, particularly catalytic reactions, is very important for heat and mass transfer, reaction efficiency and reactor cost of the reaction.
In the prior art, tubular reactors, flat-plate reactors and sleeve reactors are widely used, but the tubular reactors, the flat-plate reactors and the sleeve reactors have the problems of lower heat transfer and mass transfer efficiency, poor compactness and the like, and particularly the problems of uneven heat distribution in the reactors of the conventional reactors occur when the sizes of the reactors are required to be enlarged along with the increase of the flow rate of reaction materials. When exothermic reaction or endothermic reaction is carried out, larger temperature distribution is generated in the catalyst packed bed, so that partial catalyst has overhigh local temperature, and partial catalyst particles are sintered due to high temperature, so that larger sintered blocks are easy to form, and the increase of material flow resistance and the non-uniformity of material flow distribution are caused; meanwhile, in the use process, the catalyst particles are gradually pulverized, so that the compaction phenomenon of the catalyst filling layer can be caused, the filling height of the catalyst is obviously reduced, and the reaction performance of the catalyst is obviously reduced.
On the other hand, in the context of dual carbon targets, hydrogen energy and fuel cell technology are regarded as very promising new energy technologies, and in-vehicle methanol hydrogen production technology is paid attention to, which puts high demands on the performance, compactness and cost of the methanol hydrogen production reactor.
Disclosure of Invention
The invention mainly aims to provide a reactor and application thereof, and aims to solve the technical problems of providing a reactor which has compact structure, good heat and mass transfer performance and low cost, thereby being more practical.
The aim and the technical problems of the invention are realized by adopting the following technical proposal. According to the present invention, there is provided a reactor comprising:
a metal housing including oppositely disposed first and second faces;
a metal tube bundle disposed within the metal shell; the metal tube bundle comprises metal tubes which are arranged in parallel; the number of the metal pipes is more than or equal to 2; the two ends of each metal tube are respectively connected to the first surface and the second surface; the metal shell comprises a material inlet and a material outlet; the material inlet and the material outlet are arranged on the radial outer side of the metal tube bundle and are respectively arranged on the upstream and the downstream of the metal tube bundle; a shell pass is formed between the inner wall of the shell and the outer wall of the metal tube; the inner cavity of the metal tube forms a tube side; the shell side is filled with a granular first catalyst, and/or the tube side is filled with a granular second catalyst and/or a honeycomb second catalyst;
the metal fins are arranged on the outer wall of the metal tube, wherein the number of the metal fins on each metal tube is more than or equal to 2; the metal fins and the length direction of the metal tube form an included angle alpha, and the included angle alpha is more than 0 degrees and less than 180 degrees; the metal fins divide the shell side into at least 9 intervals communicating with each other; after the first material input into the shell side from the material inlet is reacted through the interval, a first product is output through the material outlet; and/or, after the second material input from one end of the metal pipe is reacted through the pipe side, outputting a second product through the other end of the metal pipe; when the reactor is operated, the flow direction of the materials in the metal tube bundle in the shell pass is perpendicular to the length direction of the metal tube.
The aim and the technical problems of the invention can be further realized by adopting the following technical measures.
Preferably, in the foregoing reactor, the number of metal fins on each metal tube is equal, and positions of the metal fins on adjacent metal tubes are aligned with each other.
Preferably, the aforementioned reactor further comprises a material distributor; the material distributor is arranged in the shell at the downstream of the material inlet and at the upstream of the metal tube bundle and is used for distributing the material input by the material inlet to the interval.
Preferably, the number of the metal pipes in the reactor is more than or equal to 4; the number of the metal tubes of the metal tube bundles in the horizontal direction and the vertical direction is more than or equal to 2.
Preferably, in the foregoing reactor, the metal pipe is a circular metal pipe, and the pipe outer diameter thereof is 4mm to 32mm.
Preferably, in the reactor, the metal fins are square fins, the thickness of the metal fins is 0.2-2 mm, the side length of the metal fins is 8-60 mm, and the spacing between the metal fins is 2-20 mm; the side lengths of the metal fins are parallel to each other; the first catalyst particles have a size smaller than the spacing of the metal fins and smaller than the spacing between adjacent metal tubes so that the first catalyst particles can be packed in the space.
Preferably, the foregoing reactor, wherein a set of metal tube bundles are disposed within the shell; the outsides of the first surface and the second surface are provided with tube side tube boxes; each metal pipe is connected in parallel through a tube side tube box.
Preferably, the foregoing reactor, wherein at least two sets of metal tube bundles are disposed within the shell; the outsides of the first surface and the second surface are provided with tube side tube boxes; the metal tube bundles are connected in series or in parallel through tube side tube boxes.
Preferably, in the foregoing reactor, the metal fin forms an angle of 90 ° with the length direction of the metal tube.
Preferably, the aforementioned reactor further comprises a shell side particle support orifice plate; the shell-side particle support pore plate is arranged at the downstream of the metal tube bundle and the upstream of the material outlet in the shell and is used for supporting the granular first catalyst in the shell side.
The aim of the invention and the technical problems are also achieved by adopting the following technical proposal. According to the coupling reaction method using the reactor provided by the invention, the shell side is filled with the granular first catalyst, and the first material input from the material inlet is subjected to endothermic reaction through the interval; the tube pass is filled with a granular second catalyst and/or a honeycomb second catalyst, and a second material input from one end of the metal tube is subjected to exothermic reaction through the tube pass; the exothermic reaction of the tube side is coupled with the endothermic reaction of the shell side, and heat energy is supplied to the endothermic reaction of the shell side.
The aim of the invention and the technical problems are also achieved by adopting the following technical proposal. According to the invention, the reactor is applied to the technical fields of chemistry, chemical metallurgy, environmental protection or hydrogen energy and fuel cells.
By means of the technical scheme, the reactor and the application thereof provided by the invention have at least the following advantages:
the reactor and the application thereof adopt the structural design that a metal tube bundle provided with a plurality of metal fins is accommodated in a metal shell, a shell pass is formed between the inner wall of the shell and the outer wall of the metal tube, and a tube pass is formed by the inner cavity of the metal tube; heat transfer is enhanced through a plurality of metal fins, and meanwhile, the shell side is divided into a plurality of open areas communicated with each other; rectifying the material flowing through the metal tube bundle through the interval, so that the material flowing through the shell side is uniformly distributed; filling a granular first catalyst in each open space in a shell side so that a chemical reaction occurs when a first material flows through the open space; by controlling the installation direction of the metal fins, the flowing direction of the reaction air flow flowing through the metal tube bundles in the shell pass is intersected with the length direction of the metal tubes at right angles, so that the particles of the first catalyst are well dispersed, segmented and supported, and are not easy to break, sinter and pack, and the volume utilization rate, heat transfer and mass transfer efficiency of the reactor are high; and the structural design can lead the resistance of the reaction gas flow to be small, is not easy to generate local blockage, can ensure the uniform temperature and gas flow distribution of the first catalyst packed bed, reduces the flowing dead angle and wall flow, and provides more choices for the amplification of the reactor.
Furthermore, when the endothermic reaction is carried out in the shell side and the exothermic reaction is carried out in the tube side, the reaction heat of the two reactions can be well coupled, and better energy utilization is realized.
Furthermore, the metal tube bundles are divided into a plurality of groups and connected through the tube side tube boxes, so that a series connection relationship between the metal tube bundles can be formed, and the effect of countercurrent heat exchange between the first material and the second material is achieved.
Furthermore, the metal tube can also play a role of a reinforcing rib. Furthermore, as the metal fins and the metal tube bundles containing the metal fins can be produced in a high-efficiency and mass mode by adopting a mold and other processes, the reactor provided by the invention has the remarkable advantages of good performance, high compactness and low cost.
The foregoing description is only an overview of the present invention, and is intended to provide a better understanding of the present invention, as it is embodied in the following description, with reference to the preferred embodiments of the present invention and the accompanying drawings.
Drawings
FIG. 1 is a schematic view of the structure of a reactor according to the present invention;
FIG. 2 is a schematic view of the structure of a metal tube bundle in the reactor of the present invention;
FIG. 3 is a schematic diagram showing the structure of a vaporization apparatus for aqueous methanol solution in example 1 of the present invention;
FIG. 4 is a schematic structural diagram of a reaction apparatus for producing hydrogen from methanol in example 2 of the present invention;
FIG. 5 is a schematic view showing the structure of a device for the selective methanation reaction in example 3 of the present invention.
Detailed Description
In order to further describe the technical means and effects adopted by the invention to achieve the preset aim, the following description refers to a reactor and application thereof according to the invention, and specific implementation, structure, characteristics and effects thereof are described in detail below with reference to the accompanying drawings and preferred embodiments.
The present invention proposes a reactor, as shown in fig. 1 to 5, comprising a metal shell 4; the metal shell comprises a first surface 41 and a second surface 42 which are oppositely arranged and are mainly used for fixing a metal tube bundle; the reactor also comprises a metal tube bundle 1; the metal tube bundle is arranged in the metal shell; the metal tube bundle comprises a plurality of metal tubes 3 which are arranged in parallel; the number of the metal pipes is more than or equal to 2; the two ends of each metal tube are respectively connected to the first surface and the second surface; the metal shell comprises a material inlet 6 and a material outlet 10; the material inlet and the material outlet are arranged on the radial outer side of the metal tube bundle and are respectively arranged on the upstream and the downstream of the metal tube bundle; a shell pass 11 is formed between the inner wall of the shell and the outer wall of the metal tube; the inner cavity of the metal tube forms a tube side 7; the shell side is filled with a granular first catalyst, and/or the tube side is filled with a granular second catalyst and/or a honeycomb second catalyst; the reactor further comprises a plurality of metal fins 2; the metal fins are arranged on the outer wall of the metal tube, wherein the number of the metal fins on each metal tube is more than or equal to 2; the metal fins and the length direction of the metal tube form an included angle alpha, wherein alpha is more than 0 degrees and less than 180 degrees, as shown in figure 2; the metal fins divide the shell side into at least 9 intervals communicating with each other; after the first material input into the shell side from the material inlet is reacted through the interval, a first product is output through the material outlet; and/or, after the second material input by the tube side inlet 9 of the metal tube is reacted by the tube side, outputting a second product by the tube side outlet 8 of the metal tube; in order to ensure a good effect of the first catalyst in the shell side, the flow of material through the metal tube bundle should be perpendicular to the length direction of the metal tubes during operation of the reactor.
In some embodiments of the invention, the number of metal fins on each metal tube is equal, and the positions of the metal fins on adjacent metal tubes are aligned with each other. The technical purpose of the arrangement is to ensure that the material in the shell pass flows more smoothly, and the chemical reaction in the shell pass is facilitated.
In some embodiments of the present invention, the metal fin is in a planar or corrugated structure, and may be designed as appropriate according to practical situations, and the present invention is not limited in particular.
In some embodiments of the invention, the metal shell is a square shell comprising six sides; the two ends of each metal tube are respectively connected to any one group of oppositely arranged side surfaces of the square shell. The technical purpose of designing the metal shell into the square shell is that the metal shell is convenient to manufacture, the length of each metal tube in the metal tube bundle is the same, each section in the metal tube bundle can be uniformly arranged, after the first material is input through the material inlet, the first material can be uniformly distributed from the material inlet to the material outlet, and the material flowing direction is free from disturbance or has less disturbance, so that the uniformity of chemical reaction in the shell pass is ensured.
In some embodiments of the invention, the metal shell is a square shell; the material inlet and the material outlet can be arranged on the non-opposite side surfaces of the square shell according to engineering practical conditions so as to adapt to the space complexity in different practical application scenes.
In some embodiments of the present invention, for practical purposes, a part of the side surface of the metal shell may be designed to be an arched side surface, so as to adapt to the mechanical performance requirements under different conditions of the scene.
In some embodiments of the invention, the reactor further comprises a material distributor 13; the material distributor is arranged in the shell at the downstream of the material inlet and at the upstream of the metal tube bundle and is used for distributing the material input by the material inlet to the interval. The technical design aims at uniformly distributing the first material so as to ensure that the material in the shell side has better uniformity; the design is particularly suitable for application scenes with methanol aqueous solution as the first material, and is more beneficial to uniform distribution of the first material.
In some embodiments of the invention, the number of the metal tubes is greater than or equal to 4; the number of the metal tubes of the metal tube bundles in the horizontal direction and the vertical direction is more than or equal to 2. The technical design aims to divide the shell side into a plurality of open sections with smaller volumes, ensure that a first material can smoothly pass through the metal tube bundles and divide a first catalyst into small spaces so as to realize the technical purposes of well dispersing, dividing and supporting the first catalyst, and simultaneously well avoid or reduce the first catalyst from being broken, sintered and piled, and improve the volume utilization rate and the heat and mass transfer efficiency of the reactor.
In some embodiments of the present invention, the metal tube is a circular metal tube having an outer diameter of 4mm to 32mm and a wall thickness of 0.5mm to 1.2mm, which may be determined according to the magnitude of the pressure used. In the invention, the pipe diameter of the metal pipe is smaller, the pipe cavity is not used as a place for main chemical reaction, and in fact, one of the main technical purposes of the pipe pass is to provide external heat energy for the chemical reaction in the shell pass, wherein the chemical reaction does not occur in the pipe pass at any time, but high-temperature flue gas is directly introduced as an external heat source to provide heat energy for the chemical reaction in the shell pass; sometimes, chemical reaction can also occur in the tube side, so that exothermic reactions such as combustion reaction and the like occur in the tube side, thereby providing heat energy for the chemical reaction in the shell side; meanwhile, another main technical purpose of the metal tube is to play a role of reinforcing ribs, and when the chemical reaction in the shell pass does not need external heat energy, the metal tube bundle plays a role of dispersing, dividing and supporting the first catalyst and the reinforcing ribs.
In some embodiments of the invention, the metal tube has a tube length of 50-1000 mm; the tube length can be appropriately adjusted according to the size of the reactor.
In some specific embodiments of the invention, the metal fins are square fins with the thickness of 0.2-2 mm and the side length of 8-60 mm, and the spacing of the metal fins is 2-20 mm; the side lengths of the metal fins are parallel to each other. When the metal fins are arranged into square fins, the gaps between the adjacent metal fins can be well controlled, so that adjacent open areas can be well separated to keep the first catalyst to have a good effect. The spacing of the metal fins is limited not to be too large, so that the large volume of a single open area is avoided, and the performance maintenance of the first catalyst is not facilitated; meanwhile, the distance between the metal fins is not too small, so that the material in the shell pass flows smoothly. In order to ensure that the first catalyst particles can smoothly fill the interval, the size of the first catalyst particles is smaller than the spacing of the metal fins and smaller than the spacing between adjacent metal tubes at the same time.
In some embodiments of the invention, a set of metal tube bundles are disposed within the housing; the outer sides of the first surface and the second surface are respectively provided with a tube side tube box 5; each metal pipe is connected in parallel through a tube side tube box; the technical purpose of the device is to flexibly adjust different requirements of different chemical reactions on external heat energy, and to better control energy utilization.
In some embodiments of the invention, at least two sets of metal tube bundles are disposed within the housing; the outsides of the first surface and the second surface are provided with tube side tube boxes; the metal tube bundles are connected in series or in parallel through tube side tube boxes.
In some embodiments of the present invention, the metal fin forms an angle of 90 ° with the length direction of the metal tube; the technical design aims at enabling the section shape of the open section to be rectangular, so that the resistance to the material flowing through the metal tube bundles is smaller, partial blockage is not easy to occur, the temperature and the air flow distribution of the first catalyst packed bed can be ensured to be uniform, the flowing dead angle and the wall flow are reduced, and the technical effect is better.
The metal shell, the metal tube, the metal fin and the tube side tube box can be made of different stainless steel or common carbon steel according to the use temperature.
In some embodiments of the invention, the reactor further comprises a shell side particle support orifice plate 12; the shell side particle supporting pore plate is arranged at the downstream of the metal tube bundle in the shell and at the upstream of the material outlet and is used for supporting the granular first catalyst in the shell side and avoiding the effect of influencing the reactor due to the fact that part of the first catalyst is carried during the output of the reaction gas flow.
The aim of the invention and the technical problems are also achieved by adopting the following technical proposal. According to the coupling reaction method using the reactor provided by the invention, the shell side is filled with the granular first catalyst, and the first material input by the material inlet undergoes endothermic reaction when passing through the interval; the tube pass is filled with a granular second catalyst and/or a honeycomb second catalyst, and a second material input by a tube pass inlet at one end of the metal tube undergoes an exothermic reaction when passing through the tube pass; the exothermic reaction of the tube side can be mutually coupled with the endothermic reaction of the shell side, namely, the exothermic reaction of the tube side can supply heat energy for the endothermic reaction of the shell side, so that the energy resource optimization utilization is better realized. The metal tube bundles are divided into a plurality of groups and connected through the tube side tube boxes, so that a series connection relationship between the metal tube bundles can be formed, and the countercurrent heat exchange effect between the first material and the second material is achieved.
The aim of the invention and the technical problems are also achieved by adopting the following technical proposal. According to the application of the reactor in the technical fields of chemistry, chemical engineering metallurgy, environmental protection or hydrogen energy and fuel cells, the reactor can be used in various application scenes in the technical fields.
The invention will be further described with reference to specific examples, which are not to be construed as limiting the scope of the invention, but rather as falling within the scope of the invention, since numerous insubstantial modifications and adaptations of the invention will now occur to those skilled in the art in light of the foregoing disclosure.
Unless otherwise indicated, materials, reagents, and the like referred to below are commercially available products well known to those skilled in the art; unless otherwise indicated, the methods are all methods well known in the art. Unless otherwise defined, technical or scientific terms used should be given the ordinary meaning as understood by one of ordinary skill in the art to which this invention belongs.
Example 1:
this embodiment is a vaporization apparatus for aqueous methanol solution. The specific structure is shown in figure 3.
The vaporization device of the methanol aqueous solution is applied to the reactor, and comprises a square metal shell 4; the metal shell comprises a top surface, a bottom surface and four side surfaces; the metal tube bundle 1 is arranged in the metal shell; the metal tubes forming the metal tube bundle comprise 12 metal tubes, wherein four layers are arranged from top to bottom, each layer comprises three metal tubes from front to back, and the specific arrangement structure is shown in figure 2; two ends of each metal tube are respectively connected to the left side surface and the right side surface of the metal shell; the outer diameter of the metal pipe is 30mm, the wall thickness is 1mm, and the length of the pipe is 465mm; the space between the inner wall of the metal shell and the outer wall of the metal tube is the vaporization section shell side 14; tube side tube boxes 5 are arranged outside the left side surface and the right side surface of the metal shell; the 12 metal tubes forming the metal tube bundle are connected in parallel through tube side tube boxes at two sides; a tube side inlet 9 is arranged on the left tube side box, and a tube side outlet 8 is arranged on the right tube side box; the inner cavity of the metal tube is a tube side 7 filled with a granular catalytic combustion catalyst; the second material input by the tube side inlet is subjected to combustion reaction in the tube side, the second product is output by the tube side outlet, and the metal tube supplies heat to the shell side through heat radiation of the tube wall. The outer wall of each metal tube is provided with square flat plate-shaped metal fins, one group of opposite sides of each metal fin are horizontally arranged, the other group of opposite sides of each metal fin are vertically arranged, and the included angle between each metal fin and each metal tube is 90 degrees; the number of the metal fins on each metal tube is 22, and the distance between the adjacent metal fins is 18mm; the positions of the metal fins on adjacent metal tubes are aligned with each other; the thickness of the metal fin is 1mm, and the side length is 60mm; the pipe axial spacing of two adjacent metal pipes in the horizontal direction and the vertical direction is 62mm; the shell side is divided into a plurality of sections communicated with each other by the metal tube bundles and the metal fins; corundum balls with the average diameter of 5mm are filled in each interval; a material inlet 6 is arranged in the middle of the top surface of the metal shell; the downstream of the material inlet is connected in series with a material distributor 13; the material distributor is arranged above the metal shell, the bottom surface size of the material distributor is slightly smaller than the top surface size of the metal shell, and a plurality of evenly distributed discharging holes are formed in the bottom surface of the material distributor, so that the first material can be evenly distributed, the flow direction of the first material is stable when the first material enters the metal tube bundle, and disturbance such as material direction change and the like is reduced; a shell-side particle supporting pore plate 12 is arranged below the metal tube bundle and is used for supporting particles filled in each section in the shell side so as to prevent the particles from being carried by air flow to cause loss; a material outlet 10 is arranged in the middle of the bottom surface of the metal shell; the material outlet is arranged below the shell side particle supporting pore plate; the first material is a methanol water solution, the first material is input into a shell side through a material inlet, and is distributed through a material distributor and then enters each interval for vaporization, and the obtained mixed gas of methanol steam and water steam is output through a material outlet; the second material is a mixture of methanol vapor, water vapor and air.
The metal shell, the metal tube, the metal fin and the tube side tube box are made of 304 stainless steel.
Example 2:
this example is a methanol steam reforming reaction device. The specific structure is shown in figure 4.
The methanol steam reforming reaction device adopts the reactor of the invention, and comprises a square metal shell 4; the metal shell comprises a top surface, a bottom surface and four side surfaces; the metal tube bundle 1 is arranged in the metal shell; the metal tubes forming the metal tube bundle comprise 12 metal tubes, wherein four layers are arranged from top to bottom, each layer comprises three metal tubes from front to back, and the specific arrangement structure is shown in figure 2; two ends of each metal tube are respectively connected to the left side surface and the right side surface of the metal shell; the outer diameter of the metal pipe is 16mm, the wall thickness is 1mm, and the length of the pipe is 170mm; the space between the inner wall of the metal shell and the outer wall of the metal tube is a methanol steam reforming reaction part shell pass 15; tube side tube boxes 5 are arranged outside the left side surface and the right side surface of the metal shell; the 12 metal tubes forming the metal tube bundle are connected in parallel through tube side tube boxes at two sides; a tube side inlet 9 is arranged on the left tube side box, and a tube side outlet 8 is arranged on the right tube side box; the inner cavity of the metal tube is a tube side 7 filled with a honeycomb catalytic combustion catalyst; the second material input by the tube side inlet is subjected to combustion reaction in the tube side, the second product is output by the tube side outlet, and the metal tube supplies heat to the shell side through the tube wall. The outer wall of each metal tube is provided with square flat plate-shaped metal fins, one group of opposite sides of each metal fin are horizontally arranged, the other group of opposite sides of each metal fin are vertically arranged, and the included angle between each metal fin and each metal tube is 90 degrees; the number of the metal fins on each metal tube is 22, and the distance between the adjacent metal fins is 6mm; the positions of the metal fins on adjacent metal tubes are aligned with each other; the thickness of the metal fin is 0.8mm, and the side length dimension is 35mm; the pipe axial distance between two adjacent metal pipes in the horizontal direction and the vertical direction is 37mm; the shell side is divided into a plurality of sections communicated with each other by the metal tube bundles and the metal fins; each zone is filled with a cylindrical methanol steam reforming catalyst with the average diameter and the height of 3.5 mm; a material inlet 6 is arranged in the middle of the top surface of the metal shell; a shell-side particle supporting pore plate 12 is arranged below the metal tube bundle and is used for supporting particles filled in each section in the shell side so as to prevent the particles from being carried by air flow to cause loss; a material outlet 10 is arranged in the middle of the bottom surface of the metal shell; the material outlet is arranged below the shell side particle supporting pore plate; the first material is mixed gas of methanol steam and water vapor, or the first material is methanol water solution; the first material is input into the shell side through the material inlet, then enters each interval to carry out chemical reaction or vaporization and chemical reaction, and the obtained methanol steam reforming hydrogen is output through the material outlet. The second material is methanol vapor, a mixture of water vapor and air, or a mixture of methanol vapor reforming hydrogen and air, or a mixture of anode tail gas of the fuel cell and air.
The metal shell, the metal tube, the metal fin and the tube side tube box are made of 304 stainless steel.
Example 3:
this example is a selective methanation reaction unit. The specific structure is shown in figure 5.
The reactor disclosed by the invention is applied to the selective methanation reaction device, and comprises a square metal shell 4; the metal shell comprises a top surface, a bottom surface and four side surfaces; the metal tube bundle 1 is arranged in the metal shell; the metal tubes composing the metal tube bundle comprise 6 metal tubes, wherein the metal tubes are arranged into two layers from top to bottom, each layer comprises three metal tubes from front to back, and the metal tubes are specifically arranged into a structure of 2 multiplied by 3; two ends of each metal tube are respectively connected to the left side surface and the right side surface of the metal shell; the outer diameter of the metal pipe is 6mm, the wall thickness is 0.8mm, and the length of the pipe is 170mm; the space between the inner wall of the metal shell and the outer wall of the metal tube is a methanation reaction part shell pass 16; the inner cavity of the metal tube is a tube side 7, and no filler is filled in the tube side; the metal tube bundles only play a role in dispersing, dividing and supporting the catalyst and reinforcing ribs. The outer wall of each metal tube is provided with square flat plate-shaped metal fins, one group of opposite sides of each metal fin are horizontally arranged, the other group of opposite sides of each metal fin are vertically arranged, and the included angle between each metal fin and each metal tube is 90 degrees; the number of the metal fins on each metal tube is 22, and the distance between the adjacent metal fins is 6mm; the positions of the metal fins on adjacent metal tubes are aligned with each other; the thickness of the metal fin is 0.8mm, and the side length is 35mm; the pipe axial distance between two adjacent metal pipes in the horizontal direction and the vertical direction is 37mm; the shell side is divided into a plurality of sections communicated with each other by the metal tube bundles and the metal fins; each zone is filled with a spherical selective methanation catalyst with the average diameter of 2.5 mm; a material inlet 6 is arranged in the middle of the top surface of the metal shell; a shell-side particle supporting pore plate 12 is arranged below the metal tube bundle and is used for supporting particles filled in each section in the shell side so as to prevent the particles from being carried by air flow to cause loss; a material outlet 10 is arranged in the middle of the bottom surface of the metal shell; the material outlet is arranged below the shell side particle supporting pore plate; the first material is methanol steam reforming hydrogen, which is input into the shell side through a material inlet, then enters each interval for chemical reaction, and the obtained methanol hydrogen production gas is output through a material outlet.
The metal shell, the metal tube, the metal fin and the tube side tube box are made of 304 stainless steel.
The technical features of the claims and/or the description of the present invention may be combined in a manner not limited to the combination of the claims by the relation of reference. The technical scheme obtained by combining the technical features in the claims and/or the specification is also the protection scope of the invention.
The above description is only of the preferred embodiments of the present invention, and is not intended to limit the present invention in any way, but any simple modification, equivalent variation and modification made to the above embodiments according to the technical substance of the present invention still fall within the scope of the technical solution of the present invention.
Claims (12)
1. A reactor, characterized in that it comprises:
a metal housing including oppositely disposed first and second faces;
a metal tube bundle disposed within the metal shell; the metal tube bundle comprises metal tubes which are arranged in parallel; the number of the metal pipes is more than or equal to 2; the two ends of each metal tube are respectively connected to the first surface and the second surface; the metal shell comprises a material inlet and a material outlet; the material inlet and the material outlet are arranged on the radial outer side of the metal tube bundle and are respectively arranged on the upstream and the downstream of the metal tube bundle; a shell pass is formed between the inner wall of the shell and the outer wall of the metal tube; the inner cavity of the metal tube forms a tube side; the shell side is filled with a granular first catalyst, and/or the tube side is filled with a granular second catalyst and/or a honeycomb second catalyst;
the metal fins are arranged on the outer wall of the metal tube, wherein the number of the metal fins on each metal tube is more than or equal to 2; the metal fins and the length direction of the metal tube form an included angle alpha, and the included angle alpha is more than 0 degrees and less than 180 degrees; the metal fins divide the shell side into at least 9 intervals communicating with each other; after the first material input into the shell side from the material inlet is reacted through the interval, a first product is output through the material outlet; and/or, after the second material input from one end of the metal pipe is reacted through the pipe side, outputting a second product through the other end of the metal pipe; when the reactor is operated, the flow direction of the materials in the metal tube bundle in the shell pass is perpendicular to the length direction of the metal tube.
2. The reactor of claim 1 wherein the number of metal fins on each of said metal tubes is equal and the positions of metal fins on adjacent ones of said metal tubes are aligned with each other.
3. The reactor of claim 1, further comprising a material distributor; the material distributor is arranged in the shell at the downstream of the material inlet and at the upstream of the metal tube bundle and is used for distributing the material input by the material inlet to the interval.
4. The reactor according to claim 1, wherein the number of the metal tubes is not less than 4; the number of the metal tubes of the metal tube bundles in the horizontal direction and the vertical direction is more than or equal to 2.
5. The reactor according to claim 1, wherein the metal tube is a circular metal tube having an outer diameter of 4mm to 32mm.
6. The reactor according to claim 1, wherein the metal fins are square fins having a thickness of 0.2 to 2mm and a side length of 8 to 60mm, and the metal fins have a pitch of 2 to 20mm; the side lengths of the metal fins are parallel to each other; the first catalyst particles have a size smaller than the spacing of the metal fins and smaller than the spacing between adjacent metal tubes so that the first catalyst particles can be packed in the space.
7. The reactor of claim 1, wherein a set of metal tube bundles are disposed within the shell; the outsides of the first surface and the second surface are provided with tube side tube boxes; each metal pipe is connected in parallel through a tube side tube box.
8. The reactor of claim 1, wherein at least two sets of metal tube bundles are disposed within the shell; the outsides of the first surface and the second surface are provided with tube side tube boxes; the metal tube bundles are connected in series or in parallel through tube side tube boxes.
9. The reactor of claim 1, wherein the metal fins form an angle of 90 ° with the length of the metal tube.
10. The reactor of claim 1, further comprising a shell side particle support orifice plate; the shell-side particle support pore plate is arranged at the downstream of the metal tube bundle and the upstream of the material outlet in the shell and is used for supporting the granular first catalyst in the shell side.
11. A coupling reaction process using the reactor of any one of claims 1 to 10, wherein the shell side is filled with a particulate first catalyst and the first material fed from the material inlet undergoes an endothermic reaction via the zone; the tube pass is filled with a granular second catalyst and/or a honeycomb second catalyst, and a second material input from one end of the metal tube is subjected to exothermic reaction through the tube pass; the exothermic reaction of the tube side is coupled with the endothermic reaction of the shell side, and heat energy is supplied to the endothermic reaction of the shell side.
12. Use of a reactor according to claims 1 to 10 in the fields of chemistry, chemical metallurgy, environmental protection or hydrogen energy and fuel cell technology.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310321759.9A CN116492938A (en) | 2023-03-29 | 2023-03-29 | Reactor and application thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310321759.9A CN116492938A (en) | 2023-03-29 | 2023-03-29 | Reactor and application thereof |
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| Publication Number | Publication Date |
|---|---|
| CN116492938A true CN116492938A (en) | 2023-07-28 |
Family
ID=87319301
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310321759.9A Pending CN116492938A (en) | 2023-03-29 | 2023-03-29 | Reactor and application thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116492938A (en) |
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2023
- 2023-03-29 CN CN202310321759.9A patent/CN116492938A/en active Pending
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