CN113559793A - Shell-and-tube fixed bed isothermal reactor - Google Patents
Shell-and-tube fixed bed isothermal reactor Download PDFInfo
- Publication number
- CN113559793A CN113559793A CN202110961997.7A CN202110961997A CN113559793A CN 113559793 A CN113559793 A CN 113559793A CN 202110961997 A CN202110961997 A CN 202110961997A CN 113559793 A CN113559793 A CN 113559793A
- Authority
- CN
- China
- Prior art keywords
- tube
- shell
- heat exchange
- reaction gas
- box
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
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
-
- 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
Abstract
The invention discloses an isothermal axial shell-and-tube reactor, which comprises a shell, an upper tube box, an upper end enclosure, a lower end enclosure which also serves as a lower tube box, a heat exchange tube bundle and a lower fixing tube plate, wherein the upper end enclosure and the lower end enclosure which also serves as the lower tube box are respectively fixed at the upper two ends of the shell; the upper tube box and the upper floating tube plate are positioned in the middle upper part of the shell in a floating manner, the upper floating tube plate is fixedly connected with the bottom of the upper tube box, and the upper end and the lower end of the heat exchange tube bundle are fixedly connected with the upper floating tube plate and the lower fixed tube plate respectively; the first ends of the flexible reaction gas conveying pipes are connected to the upper pipe box so as to convey reaction gas to the upper pipe box, and the second ends of the flexible reaction gas conveying pipes are connected to the upper end enclosure or/shell and extend to the outside so that the outside reaction gas can enter each flexible reaction gas conveying pipe. The invention solves the problem of temperature difference thermal stress of the shell side of the traditional fixed tube plate shell-and-tube reactor.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry and natural gas chemical industry, and relates to a shell-and-tube fixed bed isothermal reactor suitable for fixed bed gas-solid phase exothermic catalytic reaction. Is particularly suitable for CO transformation reaction, methanol synthesis, glycol synthesis, methane synthesis and the like.
Background
With the development of chemical production, in order to adapt to different heat transfer requirements and heat transfer modes, various fixed bed reactors appear, wherein gaseous reaction materials are particularly utilized, and a gas-solid phase catalytic reactor for carrying out reaction through a bed layer formed by a solid catalyst is most widely applied to the chemical production.
The fixed bed reactors are mainly classified into two types, namely adiabatic type and heat exchange type, in terms of reaction principle.
The adiabatic fixed bed reactor has simple structure and wide application. However, in practical operation, the adiabatic reactor cannot achieve high efficiency, and there are two main limitations:
firstly, limitation of chemical equilibrium; for exothermic reactions, higher temperatures tend to be more detrimental to the reaction toward equilibrium, while lower temperatures tend to reduce the rate of reaction;
secondly, the temperature of a catalyst bed layer is far beyond the use range of the catalyst due to the reaction temperature rise, so that active components on the surface of the catalyst are sintered, the specific surface area is greatly reduced, the activity is reduced, side reactions are intensified, even temperature runaway is caused, and equipment is damaged; therefore, for the exothermic catalytic reaction device, to achieve deeper reaction, a multi-stage heat exchange type adiabatic bed process is usually adopted, the process is long, the heat exchange network is complex, the influence on load fluctuation and raw material gas component change is large due to the constraint of energy balance of the whole plant, and the long-term stable and safe operation of the device is not facilitated.
The isothermal reactor removes reaction heat in time by a heat exchange element, keeps the bed layer basically constant in temperature, and has the main advantages that:
firstly, isothermal operation enables an actual reaction temperature curve to be close to a maximum reaction rate curve, so that the reaction rate is greatly improved, and the reaction tends to be balanced;
secondly, the isothermal reaction provides a mild operation environment for the catalyst, so that the service life of the catalyst is prolonged;
the mode of taking away the reaction heat of the catalyst bed by utilizing the water circulation byproduct steam is proved to be effective by practice for decades, has stronger controllability, and can effectively control the temperature of the catalyst bed by adjusting the byproduct steam pressure;
the isothermal reaction effectively avoids the over-temperature phenomenon of the catalyst bed layer, simultaneously avoids side reactions possibly generated by certain reactions, and improves the safety of the device.
With the characteristics of large-scale devices, diversified coal gasification technologies and the like, the use of the isothermal reactor or the combined use of the isothermal reactor and the adiabatic reactor can be more suitable for the requirements of certain processes.
In the prior art, a common axial isothermal reactor is a fixed tube-plate isothermal tubular reactor, a catalyst is filled in a heat exchange tube, a tube plate is welded with a shell, reaction gas flows in the tube along the axial direction, and water vapor on the shell side removes reaction heat and produces steam as a byproduct. Considering the problem of shell-side temperature difference, the heat exchange tube is made of dual-phase steel, and the catalyst is supported by alumina balls in the lower tube box. But the problems of failure of the pipe joint of the heat exchange pipe, cracking of the pipe plate, failure of the welding line between the pipe plate and the shell and the like caused by the inconsistent deformation of the heat exchange pipe and the pipe plate occur in engineering practice; meanwhile, along with the enlargement of the specification of the reactor, a large amount of alumina balls are used, so that the problems of heavy equipment operation weight, difficult catalyst replacement and the like are caused.
Object of the Invention
The invention discloses an isothermal axial shell-and-tube reactor aiming at the problems of the prior fixed tube-plate isothermal tubular reactor.
In order to achieve the purpose, the invention adopts the technical scheme that:
an isothermal axial shell-and-tube reactor comprises a shell, an upper tube box, an upper head, a lower head serving as a lower tube box, a heat exchange tube bundle and a lower fixed tube plate, wherein the upper head and the lower head serving as the lower tube box are respectively fixed at the upper end and the lower end of the shell in the axial direction; the lower fixed tube plate is fixed between the lower end of the shell in the axial direction and the lower end socket which is also used as a lower tube box, and the lower fixed tube plate is characterized by further comprising an upper tube box, a plurality of flexible reaction gas conveying pipes and an upper floating tube plate, wherein the upper tube box and the upper floating tube plate are positioned in the middle upper part of the shell in a floating mode, the upper floating tube plate is fixedly connected with the bottom of the upper tube box, and the upper end and the lower end of the heat exchange tube bundle are respectively fixedly connected with the upper floating tube plate and the lower fixed tube plate and are parallel to the axial line of the shell; the first ends of the flexible reaction gas conveying pipes are connected to the upper pipe box so as to convey reaction gas to the upper pipe box, and the second ends of the flexible reaction gas conveying pipes are connected to the upper end enclosure or/and the shell and extend to the outside so that the outside reaction gas can enter each flexible reaction gas conveying pipe.
In a preferred embodiment of the present invention, a plurality of heat exchange tube support plates are arranged in the shell between the upper floating tube plate and the lower fixed tube plate at intervals along the axial direction of the shell, each heat exchange tube support plate is provided with a number of heat exchange tube holes equal to the number of heat exchange tubes in the heat exchange tube bundle, the outer periphery of each heat exchange tube support plate is fixedly connected with the shell, each heat exchange tube in the heat exchange tube bundle penetrates through the corresponding heat exchange tube hole in each heat exchange tube support plate, and the outer diameter of each heat exchange tube is in sliding fit with the inner diameter of the corresponding heat exchange tube hole.
In a preferred embodiment of the present invention, each heat exchange tube supporting plate is provided with a water passage hole.
In a preferred embodiment of the present invention, a plurality of flexible reaction gas conveying pipes are bent and coiled to the upper channel box along the inside of the upper header and the inside of the shell, leaving an intermediate channel space.
In a preferred embodiment of the present invention, the number of the flexible reactant gas delivery pipes is four, first ends of the four flexible reactant gas delivery pipes are uniformly distributed and connected to the upper tube box so as to deliver reactant gas to the upper tube box, second ends of every two flexible reactant gas delivery pipes are connected in parallel and then connected to a reactant gas pipe joint, and two reactant gas pipe joints are uniformly distributed and connected to the upper end enclosure or/the housing and extend to the outside so that the outside reactant gas can enter each flexible reactant gas delivery pipe.
In a preferred embodiment of the present invention, each heat exchange tube is filled with a catalyst, and a catalyst support structure is disposed at the bottom of the lower fixed tube plate to support the catalyst in each heat exchange tube.
In a preferred embodiment of the invention, a compressed wire mesh is provided within the section of each heat exchange tube in the lower fixed tube sheet to support the catalyst within each heat exchange tube, the compressed wire mesh being supported at its lower end on the catalyst support structure.
In a preferred embodiment of the invention, the catalyst support structure is a V-shaped mesh catalyst support structure; the V-shaped mesh catalyst supporting structure comprises a plurality of V-shaped meshes and a plurality of supporting plates, wherein a plurality of V-shaped grooves are formed in each supporting plate, all the supporting plates are fixed on the inner wall of the lower end socket which is also used as the lower pipe box, and each V-shaped mesh is clamped into the V-shaped groove corresponding to all the supporting plates.
In a preferred embodiment of the invention, a V-shaped mesh gap is left between adjacent V-shaped meshes, which allows air to flow without the catalyst falling.
In a preferred embodiment of the present invention, all the V-shaped nets and all the supporting plates may be combined in a split structure or may be fixed to form a whole.
Compared with the traditional fixed tube plate shell-and-tube reactor, the invention firstly solves the problem of temperature difference and thermal stress of the shell side of the traditional fixed tube plate shell-and-tube reactor by adopting the technical scheme that the lower fixed tube plate is fixedly connected with the shell, the upper floating tube plate is fixedly connected with the upper tube box, the upper tube box is arranged in the shell in a floating way and is connected with the upper end enclosure through the flexible reaction gas conveying pipe, and the shell, the upper floating tube plate, the lower fixed tube plate, the upper tube box and the heat exchange tube bundle form a basic element for heat transfer. Compared with the traditional fixed tube plate reactor, the temperature difference stress and the deformation of the fixed tube plate reactor can be released, the failure problems of a heat exchange tube joint, a tube plate welding seam and the like are avoided, and the reliability of equipment is enhanced. And secondly, the problem that the traditional fixed tube plate shell-and-tube reactor usually adopts a dual-phase steel material and controls the reaction temperature below 300 ℃ in order to reduce the thermal expansion difference between the heat exchange tube and the shell is solved. The invention can reduce material selection, only need to select material according to the corrosion characteristic of the reaction gas, and can accept chemical reaction with larger temperature difference.
In addition, the section of each heat exchange tube positioned in the lower fixed tube plate is internally provided with the compressed metal wire mesh and is matched with the V-shaped mesh catalyst supporting structure arranged at the bottom of the lower fixed tube plate, so that the catalyst can be well supported, the gas circulation is not influenced, the problem that the traditional reactor supports the catalyst by adopting a large amount of accumulated alumina balls is solved, the operation weight of the reactor is greatly reduced, and the problem that the alumina balls are difficult to sort and the like during the catalyst unloading is solved. The V-shaped net further has high strength and controllable aperture ratio and can be installed in blocks.
Drawings
FIG. 1 is a schematic structural view of an isothermal axial shell-and-tube reactor of the present invention.
Fig. 2 is an enlarged schematic view at I of fig. 1.
Fig. 3 is a sectional view a-a of fig. 2.
Fig. 4 is a sectional view B-B of fig. 2.
Fig. 5 is a schematic of the catalyst within the heat exchange tubes of the present invention supported by a compressed wire mesh and V-mesh catalyst support structure.
FIG. 6 is a schematic perspective view of a V-shaped mesh catalyst support structure of the present invention.
FIG. 7 is a front view of a V-shaped mesh catalyst support structure of the present invention.
FIG. 8 is a top view of a V-shaped mesh catalyst support structure of the present invention.
Detailed Description
The invention is further described below in conjunction with the appended drawings and detailed description.
Referring to fig. 1, the isothermal axial shell-and-tube reactor shown in the figure comprises a shell 10, an upper head 30, a lower head 40 also used as a lower tube box, a heat exchange tube bundle 50 and a lower fixed tube plate 60, wherein the upper head 30 and the lower head 40 also used as the lower tube box are respectively fixed at the upper end and the lower end of the shell 10 in the axial direction by welding; the lower fixed tube plate 60 is fixed between the lower end of the shell 10 in the axial direction and the lower end enclosure 40 which also serves as a lower tube box, and the upper end enclosure 30 is provided with an operation manhole 31 and a plurality of saturated water vapor outlets 32.
Compared with the traditional fixed tube plate shell-and-tube reactor, the invention has the characteristics that:
the reactor also comprises an upper tube box 20, a plurality of flexible reaction gas conveying pipes 80 and an upper floating tube plate 70, wherein the upper tube box 20 and the upper floating tube plate 70 are positioned in the middle upper part of the shell 10 in a floating manner, the upper tube box 20 is in a hemispherical shell shape, and the upper floating tube plate 70 is fixedly connected with the bottom of the upper tube box 20 (or called as an inner tube box) (namely the bottom of the hemispherical shell) in a welding manner, so that a pressure-bearing cavity is defined by the upper tube box 20 and the upper floating tube plate 70. The pressure-bearing cavity should take sufficient space into consideration and provide an operation manhole 21 at the top of the upper pipe box 20, so as to facilitate catalyst filling and equipment maintenance.
The upper end and the lower end of the heat exchange tube bundle 50 are respectively fixedly connected with the upper floating tube plate 70 and the lower fixed tube plate 60 in a welding mode and are parallel to the axis of the shell 10; because the upper header 20 and the upper floating tube plate 70 are also positioned in the upper middle portion of the shell 10 in a floating manner, the thermal expansion difference between the heat exchange tube bundle 50 and the shell 10 can be absorbed, and the problem of shell-side temperature difference thermal stress of the traditional fixed tube plate shell-and-tube reactor is solved. Compared with the traditional fixed tube plate reactor, the temperature difference stress and the deformation of the fixed tube plate reactor can be released, the failure problems of a heat exchange tube joint, a tube plate welding seam and the like are avoided, and the reliability of equipment is enhanced. In addition, the problem that in order to reduce the thermal expansion difference between the heat exchange tube and the shell of the traditional fixed tube plate shell-and-tube reactor, a dual-phase steel material is usually adopted and the reaction temperature is controlled below 300 ℃ is solved. Therefore, the parts of the invention can reduce the material selection, only need to select the material according to the corrosion characteristic of the reaction gas, and can accept the chemical reaction with larger temperature difference.
In addition, an annular gap a is left between the upper floating tube plate 70 and the interior of the shell 10, which facilitates the upward flow of water vapor through the annular gap after heat exchange is completed.
In order to enable the pressure-bearing cavity enclosed by the upper tube box 20 and the upper floating tube plate 70 to float up and down, the invention adopts a plurality of flexible reaction gas conveying pipes 80 to input reaction gas into the pressure-bearing cavity enclosed by the upper tube box 20 and the upper floating tube plate 70.
In a preferred embodiment of the present invention, the number of flexible reactant gas delivery conduits 80 is four (although not limited to four, and may be one, two, three, or more than four, the number of flexible reactant gas delivery conduits 80 may be matched according to process requirements, but must have sufficient strength and absorb thermal expansion). When the flexible reaction gas delivery pipe 80 is configured, the thermal expansion difference between the heat exchange tube bundle 50 and the shell 10 should be considered, especially considering special working conditions such as starting and stopping.
Referring to fig. 2 to 4 in particular, first ends of four flexible reactant gas delivery pipes 80 are connected to the upper pipe box 90 in an evenly distributed manner so as to feed reactant gas into a pressure-bearing cavity defined by the upper pipe box 20 and the upper floating pipe plate 70, second ends of every two flexible reactant gas delivery pipes 80 are connected in parallel and then connected to a reactant gas pipe joint 81, and two reactant gas pipe joints 81 are connected to the upper head 30 in an evenly distributed manner and extend to the outside (of course, they may be connected to the housing 10 in an evenly distributed manner and extend to the outside) so that the outside reactant gas enters each flexible reactant gas delivery pipe 80.
The first ends of the four flexible reaction gas conveying pipes 80 are all provided with reaction gas inlet distributors 82, and the reaction gas is uniformly distributed through the reaction gas inlet distributors 82 and enters a pressure-bearing cavity defined by the upper tube box 20 and the upper floating tube plate 70.
Four flexible reaction gas delivery pipes 80 are bent and coiled along the inside of the upper header 30 and the inside of the shell 10 to the upper header 20, leaving a middle passage space for catalyst filling and equipment maintenance.
With reference to fig. 1, a plurality of heat exchange tube support plates are arranged in the shell 10 between the upper floating tube plate 70 and the lower fixed tube plate 60 at intervals along the axial direction of the shell 10, each heat exchange tube support plate 100 is provided with a plurality of heat exchange tube holes (not shown in the figure) with the same number as that of the heat exchange tubes 51 in the heat exchange tube bundle 50, the outer periphery of each heat exchange tube support plate 100 is fixedly connected with the shell 10 in a welding manner, each heat exchange tube 51 in the heat exchange tube bundle 50 penetrates through the corresponding heat exchange tube hole in the heat exchange tube support plate 100, and the outer diameter of each heat exchange tube 51 is in sliding fit with the inner diameter of the corresponding heat exchange tube hole. In addition, a water passage hole (not shown) is formed in each heat exchange tube support plate 100. Further, the plurality of heat exchange tube support plates 100 may be connected to each other by tie rods (not shown).
The present invention further includes a downcomer assembly 90, which downcomer assembly 90 has a plurality of feed water inlets (not shown) that are uniformly distributed on the shell 10 and communicate with the interior of the shell 10 in order to provide uniform shell side water vapor distribution.
A gas outlet collector 41 and an operation manhole are arranged on the lower end enclosure 40 which is also used as the lower tube box, a gas inlet of the gas outlet collector 41 is communicated with the inside of the lower end enclosure 40 which is also used as the lower tube box so as to collect reaction gas after reaction, and a gas outlet of the gas outlet collector 41 is communicated with the outside so as to be sent out of the reactor to enter the next process.
Referring to fig. 5 to 8 in combination, in order to sufficiently perform a catalytic reaction of the reaction gas entering the heat exchange tubes 51, a catalyst 52 is filled in each heat exchange tube 51.
In order to provide a good support for the catalyst 52 in each heat exchange tube 51 without affecting the gas flow, a compressed wire mesh 53 is provided in the section of each heat exchange tube 51 in the lower fixed tube plate 60, while a catalyst support structure 54 is provided at the bottom of the lower fixed tube plate 60, the compressed wire mesh 53 being used to support the catalyst 52 in each heat exchange tube 51, and the lower end of the compressed wire mesh 51 being supported on the catalyst support structure 54. The height of the compression wire mesh 51 is determined by the distance of the upper surface of the fixed tube sheet 60 to the upper surface of the catalyst support structure 54.
All the V-shaped nets 54a and all the supporting plates 54b may be combined in a split structure or may be fixed to form a whole.
Adopt the mode that above-mentioned compression wire mesh 53 and catalyst bearing structure 54 combine to play good supporting role to the catalyst, do not influence the gas circulation simultaneously, avoid traditional reactor to adopt a large amount of alumina balls of piling up to support the catalyst, both alleviateed reactor operating weight in a large number and avoided alumina balls to be difficult to the problem such as letter sorting when uninstalling the catalyst again.
The loading of the catalyst 52 of the isothermal axial shell-and-tube reactor is the same as that of the traditional tube reactor, and the unloading is realized by adopting a top vacuum suction method, so that the efficiency is high, and the dust pollution is avoided.
In order to quickly take away the reaction heat by the water vapor outside the heat exchange tubes 52 when the catalyst 50 is filled in the heat exchange tubes 51, the catalyst 50 is filled in the upper floating tube plate 70, the filling height of the shrinkage rate of the catalyst is higher than that of the upper floating tube plate 70, and the catalyst enters the lower part of the upper floating tube plate 70 after shrinkage.
The working principle of the isothermal axial shell-and-tube reactor is as follows:
the reaction gas enters into the four flexible reaction gas conveying pipes 80 from the two reaction gas pipe joints 110 arranged on the upper end enclosure 30, and is uniformly distributed and enters into a pressure-bearing cavity enclosed by the upper header 20 and the upper floating pipe plate 70 through the four flexible reaction gas conveying pipes 80 and the reaction gas inlet distributor 120. The reaction gas entering the pressure-bearing cavity enclosed by the upper tube box 20 and the upper floating tube plate 70 enters the heat exchange tubes 51 filled with the catalyst 52 for catalytic reaction. The reaction heat generated by the catalytic reaction is removed in time by the saturated water vapor outside the heat exchange tube 51.
The reaction gas enters the lower end enclosure 40 which also serves as a lower tube box after the reaction is finished through the heat exchange tube 51, and is sent out from the gas outlet of the gas outlet collector 41 to enter the next process after being collected by the gas outlet collector 41.
Meanwhile, boiler feed water and steam pocket downcomer feed water enter the shell 10 from a plurality of feed water inlets of the downcomer assembly 90 arranged at the lower part of the shell 10 in an evenly distributed manner, water vapor absorbs reaction heat in the heat exchange tubes 51 and flows from bottom to top through the water through holes in each heat exchange tube supporting plate 200, the water vapor after heat exchange continuously enters the upper end enclosure 30 from top to bottom through the annular gap between the upper floating tube plate 70 and the inside of the shell 10, and finally is sent out through a plurality of saturated water vapor outlets 32 arranged on the upper end enclosure 30 and enters steam-water separation (steam pocket) equipment.
The isothermal axial shell-and-tube reactor is used for producing 50 ten thousand tons/year methanol synthesis tower, the diameter DN4000mm of the shell 10 in the isothermal axial shell-and-tube reactor, the length 8000mm of the heat exchange tube bundle 50, and the catalyst 52 filling 52m3. The metal net weight of the isothermal axial shell-and-tube reactor is 185 tons, and the weight of the catalyst is 52 tons to 68 tons. The bottom of the catalyst 52 is not supported by alumina balls, and the operation weight can be reduced by 40 tons compared with the traditional methanol synthesis tower adopting the catalyst supported by the alumina balls. The shell side by-product is 2.5 MPag-4.0 MPag medium-pressure saturated steam (the pressure is adjustable), the reaction hot spot temperature: the thermal expansion difference between the heat exchange tube bundle 50 and the shell 10 is absorbed by the upper floating tube plate 60 and the flexible reaction gas conveying pipe 80 at the temperature of 280 ℃, and the equipment is safe and reliable.
Claims (10)
1. An isothermal axial shell-and-tube reactor comprises a shell, an upper tube box, an upper head, a lower head serving as a lower tube box, a heat exchange tube bundle and a lower fixed tube plate, wherein the upper head and the lower head serving as the lower tube box are respectively fixed at the upper end and the lower end of the shell in the axial direction; the lower fixed tube plate is fixed between the lower end of the shell in the axial direction and the lower end socket which is also used as a lower tube box, and the lower fixed tube plate is characterized by further comprising an upper tube box, a plurality of flexible reaction gas conveying pipes and an upper floating tube plate, wherein the upper tube box and the upper floating tube plate are positioned in the middle upper part of the shell in a floating mode, the upper floating tube plate is fixedly connected with the bottom of the upper tube box, and the upper end and the lower end of the heat exchange tube bundle are respectively fixedly connected with the upper floating tube plate and the lower fixed tube plate and are parallel to the axial line of the shell; the first ends of the flexible reaction gas conveying pipes are connected to the upper pipe box so as to convey reaction gas to the upper pipe box, and the second ends of the flexible reaction gas conveying pipes are connected to the upper end enclosure or/and the shell and extend to the outside so that the outside reaction gas can enter each flexible reaction gas conveying pipe.
2. An isothermal axial shell-and-tube reactor according to claim 1, wherein a plurality of heat exchange tube support plates are arranged in the shell between the upper floating tube plate and the lower fixed tube plate at intervals along the axial direction of the shell, each heat exchange tube support plate is provided with a number of heat exchange tube holes equal to the number of heat exchange tubes in the heat exchange tube bundle, the outer periphery of each heat exchange tube support plate is fixedly connected with the shell, each heat exchange tube in the heat exchange tube bundle penetrates through the corresponding heat exchange tube hole in each heat exchange tube support plate, and the outer diameter of each heat exchange tube is in sliding fit with the inner diameter of the corresponding heat exchange tube hole.
3. An isothermal axial shell and tube reactor according to claim 2, wherein a water through hole is provided in each heat exchange tube support plate.
4. An isothermal axial shell and tube reactor according to claim 1, wherein several flexible reaction gas delivery tubes are serpentine along the inside of the header and the inside of the shell to the header leaving intermediate passage spaces.
5. The isothermal axial shell-and-tube reactor according to claim 4, wherein the number of the flexible reaction gas delivery pipes is four, the first ends of the four flexible reaction gas delivery pipes are connected to the upper tube box in an evenly distributed manner so as to feed the reaction gas to the upper tube box, the second ends of every two flexible reaction gas delivery pipes are connected in parallel and then connected with a reaction gas pipe joint, and the two reaction gas pipe joints are connected to the upper end enclosure or/the shell in an evenly distributed manner and extend to the outside so as to allow the outside reaction gas to enter each flexible reaction gas delivery pipe.
6. An isothermal axial shell and tube reactor according to any of claims 1-5, wherein a catalyst is packed in each heat exchange tube, and a catalyst support structure is provided at the bottom of the lower fixed tube sheet to support the catalyst in each heat exchange tube.
7. An isothermal axial shell and tube reactor according to claim 6, wherein a compressed wire mesh is provided within the section of each heat exchange tube located in said lower fixed tube sheet, said compressed wire mesh supporting the catalyst within each heat exchange tube, said compressed wire mesh being supported at its lower end on said catalyst support structure.
8. An isothermal axial shell and tube reactor according to claim 7, wherein said catalyst support structure is a V-shaped mesh catalyst support structure; the V-shaped mesh catalyst supporting structure comprises a plurality of V-shaped meshes and a plurality of supporting plates, wherein a plurality of V-shaped grooves are formed in each supporting plate, all the supporting plates are fixed on the inner wall of the lower end socket which is also used as the lower pipe box, and each V-shaped mesh is clamped into the V-shaped groove corresponding to all the supporting plates.
9. An isothermal axial shell and tube reactor according to claim 8, wherein a V-shaped mesh gap is left between adjacent V-shaped meshes to allow air flow without catalyst drop.
10. An isothermal axial shell and tube reactor according to claim 9, characterized in that all V-shaped wires and all support plates can be combined in a split configuration or fixed as a whole.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110961997.7A CN113559793A (en) | 2021-08-20 | 2021-08-20 | Shell-and-tube fixed bed isothermal reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110961997.7A CN113559793A (en) | 2021-08-20 | 2021-08-20 | Shell-and-tube fixed bed isothermal reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113559793A true CN113559793A (en) | 2021-10-29 |
Family
ID=78172349
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110961997.7A Pending CN113559793A (en) | 2021-08-20 | 2021-08-20 | Shell-and-tube fixed bed isothermal reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113559793A (en) |
-
2021
- 2021-08-20 CN CN202110961997.7A patent/CN113559793A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105457563B (en) | Isothermal shift reactor with built-in tube bundle | |
| US8460614B2 (en) | Heat exchanger with radially arranged elements for isothermal chemical reactors | |
| CN100528320C (en) | Transverse pipe type heat transfer reaction unit | |
| US20170028373A1 (en) | Isothermal tubular catalytic reactor | |
| RU2719986C2 (en) | Isothermal catalytic tubular reactor | |
| CN203075923U (en) | Axial-radial constant-temperature conversion reactor | |
| CN102887481A (en) | Low water-gas ratio pre-conversion constant-temperature CO conversion technology | |
| CN1857766B (en) | Heat exchanging reactor | |
| US20130052097A1 (en) | Chemical Reactor with a Plate Heat Exchanger | |
| CN216063176U (en) | Shell-and-tube fixed bed isothermal reactor | |
| CN113559793A (en) | Shell-and-tube fixed bed isothermal reactor | |
| CN112044363B (en) | Coupling reactor for producing ethylene glycol from coal | |
| CN212119941U (en) | Heat transfer system of shift converter | |
| CN102205221A (en) | Fixed bed catalyst reactor having heat-exchange medium distributing and gathering structure | |
| CN216764335U (en) | Novel methanol hydrogen production device | |
| CN112705115B (en) | Fixed bed reactor | |
| CN215389173U (en) | Reactor with steam superheater arranged between multi-section radial heat insulation sections | |
| CN210700014U (en) | Dimethyl ether reactor of built-in module assembled heat exchange tube bundle | |
| CN111081397A (en) | Integrated nuclear reactor primary loop heat exchanger | |
| CN108212025B (en) | Composite tower type methanation reactor | |
| CN110975767A (en) | Double-isothermal converter with double cooling systems | |
| CN205182684U (en) | A novel reactor for hydrogen peroxide propylene epoxide makes epoxypropane | |
| CN110902650A (en) | Double-steam-drum double-isothermal conversion furnace |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |