CN108970548B - Isothermal shift reaction device - Google Patents
Isothermal shift reaction device Download PDFInfo
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- CN108970548B CN108970548B CN201811160863.XA CN201811160863A CN108970548B CN 108970548 B CN108970548 B CN 108970548B CN 201811160863 A CN201811160863 A CN 201811160863A CN 108970548 B CN108970548 B CN 108970548B
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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
- B01J8/0242—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 the fluid flow within the bed being predominantly vertical
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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
- B01J8/0285—Heating or cooling the reactor
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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
- 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
- B01J2208/00194—Tubes
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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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
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Abstract
The invention relates to an isothermal shift reaction device, which comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a synthesis gas collecting pipe is arranged in the middle of the catalyst frame, a gap is formed between the side wall of the catalyst frame and the side wall of the furnace body, and a plurality of air inlets communicated with the gap and the inner cavity of the catalyst frame are formed in the side wall of the catalyst frame; a plurality of heat exchange tubes are arranged in a catalyst bed layer space between the catalyst frame and the synthesis gas collecting tube, the heat exchange tubes are longitudinally arranged in parallel in the catalyst bed layer space, inlets of the heat exchange tubes are connected with a cooling water pipeline, and outlets of the heat exchange tubes are connected with a steam collecting pipeline; the method is characterized in that: the heat exchange tube comprises an outer tube and an inner tube, one port of the outer tube is closed, and the second port of the outer tube is communicated with the steam collecting pipeline; the inner tube inserts the outer tube from the second port of outer tube in, has the clearance between inner tube and the outer tube, the inner chamber of first port intercommunication outer tube of inner tube, the second port intercommunication cooling water pipeline of inner tube.
Description
Technical Field
The invention relates to chemical equipment, in particular to an isothermal transformation reaction device.
Background
CO + H shift reaction2O ↔H2+CO2The reaction is exothermic, the temperature of the conversion gas can reach about 450 ℃ after the reaction is completed, but the energy barrier (reaction activity) of the reaction is higher, and the reaction raw material, namely the raw gas, needs to be heated to 260 ℃ or higher before the reaction. Therefore, the prior conversion process uses a conversion gas crude gas heat exchanger, and utilizes conversion gas with high temperature generated after the conversion reaction to exchange heat with crude gas before the conversion reaction. Can save a large amount of energy sources and can greatly improve the reaction rate and efficiency. However, because the temperature at the outlet of the converter is very high, the pressure of the conversion reaction is very high, generally 3-6 MPa, and higher requirements are provided for the material and the thickness of the shell of the converter. With the further expansion of single-line production capacity of chemical engineering projects, the size of a single shift reactor is further increased, the diameter of the current large-scale shift converter can reach 4800mm, the thickness of an equipment shell reaches 110mm, the material cost and the manufacturing cost are greatly increased, and higher requirements are provided for processing technology and equipment transportation.
Because of different medium components in the shift converter, when the water-gas ratio is too low, the temperature can rise rapidly, and when the heat is not removed in time, the phenomena of temperature runaway (rapid rise of a reaction zone in equipment) and the like can occur. The methanation reaction can be caused after the temperature in the equipment is too high, when the condition occurs, the temperature in the equipment can reach 600-800 ℃, and when the working condition occurs, the catalyst loses activity due to the too high temperature, and needs to be replaced, thereby causing great economic loss. Moreover, when the temperature of the equipment wall is too high, the strength of the equipment is also sharply reduced, and a huge safety risk is brought to the production of the whole device.
In order to control the stable performance of the CO shift reaction at the designed temperature, it is generally adopted to arrange a heat exchange tube in the reactor, and to remove the heat generated by the shift reaction by passing cooling water through the heat exchange tube, thereby controlling the reaction temperature.
However, as the reaction proceeds, the catalyst activity decreases, and the catalyst activity temperature increases from about 240 ℃ to about 280 ℃, which requires a corresponding increase in the reaction temperature. The existing method for solving the problem generally increases the temperature of cooling water and heat exchange steam at the later stage of reaction, which inevitably leads to the pressure in a steam drum and a heat exchange tube to be increased sharply; and the design wall thickness of the steam pocket and the heat exchange tube is correspondingly increased. In addition to the strict requirement on equipment, a series of other problems can also be caused, for example, the heat transfer coefficient of the heat exchange tube is reduced due to the increase of the wall thickness of the heat exchange tube, and the heat exchange amount in the early stage of the reaction also needs to be increased; moreover, due to the change of the temperature and the pressure of the steam outlet drum, the corresponding change of the matched pipeline and the equipment is necessarily caused. A series of problems are brought about.
Disclosure of Invention
The invention aims to solve the technical problem of providing an isothermal shift reaction device which has sufficient heat removal and can accurately control the temperature of a catalyst bed layer aiming at the current situation of the prior art.
Another technical problem to be solved by the present invention is to provide an isothermal shift reactor which can maintain a constant yield over the entire active period of the catalyst without increasing the wall thickness of the equipment, in view of the current state of the art.
The technical scheme adopted by the invention for solving the technical problems is as follows: the isothermal transformation reaction device comprises a furnace body and a catalyst frame arranged in the furnace body, wherein a synthesis gas collecting pipe is arranged in the middle of the catalyst frame, a gap is formed between the side wall of the catalyst frame and the side wall of the furnace body, and a plurality of air inlets communicated with the gap and the inner cavity of the catalyst frame are formed in the side wall of the catalyst frame; a plurality of heat exchange tubes are arranged in a catalyst bed layer space between the catalyst frame and the synthesis gas collecting tube, the heat exchange tubes are longitudinally arranged in parallel in the catalyst bed layer space, inlets of the heat exchange tubes are connected with a cooling water pipeline, and outlets of the heat exchange tubes are connected with a steam collecting pipeline;
the method is characterized in that:
the heat exchange tube comprises an outer tube and an inner tube, one port of the outer tube is closed, and the second port of the outer tube is communicated with the steam collecting pipeline;
the inner pipe is inserted into the outer pipe from the second port of the outer pipe, a gap is formed between the inner pipe and the outer pipe, the first port of the inner pipe is communicated with the inner cavity of the outer pipe, and the second port of the inner pipe is communicated with the cooling water pipeline.
In order to further ensure the heat exchange effect, a spoiler can be arranged in the cavity between the inner pipe and the outer pipe.
Preferably, the spoiler is spirally arranged in an axial direction of the inner pipe. The structure can effectively prolong the water flow path, increase the retention time of water flow and fully exchange heat.
As a further improvement of the above solutions, each heat exchange tube may be divided into two groups, and correspondingly, there are two groups of cooling water pipelines; the inlet of each inner pipe in the first group of heat exchange pipes is connected with a first cooling water pipeline, and the inlet of each inner pipe in the second group of heat exchange pipes is connected with a second cooling water pipeline; a valve is arranged on the second cooling water pipeline; and controlling the volume flow of the refrigerant entering each inner tube in the first group of heat exchange tubes to be 4-9 times of the volume flow of the refrigerant entering each inner tube in the second group of heat exchange tubes.
The structure design overcomes the prejudice that only one group of heat exchange tubes is adopted in the prior art and the activity temperature of the catalyst at the later stage of the operation of the device is ensured by improving the steam pressure, the isothermal shift reaction device is designed into the isothermal shift reaction device with variable temperature, the design of the two groups of heat exchange tubes can change the heat removal amount according to the activity requirement of the catalyst at each stage of the operation of the device, thereby meeting the requirement of the catalyst activity temperature at different reaction stages, maintaining the constant yield, and simultaneously avoiding the problems of increased wall thickness of the heat exchange tubes, increased wall thickness of the steam pocket, changed matching pipelines and equipment and the like caused by the method that the pressure in the steam pocket and the heat exchange tubes is increased to improve the reaction temperature at the later stage of the reaction in the prior art, reducing the equipment.
Preferably, in order to ensure the uniformity of heat removal, the heat exchange tubes in the first group of heat exchange tubes can be uniformly arranged on the cross section of the catalyst bed layer space; and all the heat exchange tubes in the second group of heat exchange tubes are uniformly arranged on the cross section of the catalyst bed layer space.
Preferably, the caliber of each inner tube in the first group of heat exchange tubes is equal to the caliber of each inner tube in the second group of heat exchange tubes, and the caliber of each outer tube in the first group of heat exchange tubes is equal to the caliber of each outer tube in the second group of heat exchange tubes.
The control of the flow of the refrigerant in the two groups of heat exchange tubes can be realized by various structures, for example, the control can be realized by controlling the flow of the refrigerant entering the two groups of cooling water pipelines, or the calibers of the inner tubes in the first group of heat exchange tubes are 4-9 times of the calibers of the inner tubes in the second group of heat exchange tubes, and the calibers of the outer tubes in the first group of heat exchange tubes are 4-9 times of the calibers of the outer tubes in the second group of heat exchange tubes. The heat removed by the two groups of heat exchange tubes can be controlled by the difference of the number of the two groups of heat exchange tubes.
It is also possible that the heat exchange tubes are arranged radially in the radial direction on the cross section of the catalyst bed space.
Further, each of the heat exchange tubes is uniformly arranged on a plurality of concentric circumferential lines centered on the axis of the catalyst frame in the circumferential direction of the cross section of the catalyst bed space.
Preferably, the cross section of the catalyst bed space is divided into three areas from inside to outside, and only the heat exchange tubes in the first group of heat exchange tubes are arranged in a first area at the inner side and a third area at the outer side; the heat exchange tubes in the first group of heat exchange tubes and the heat exchange tubes in the second group of heat exchange tubes are simultaneously arranged in the second area in the middle, and the heat exchange tubes in the second group of heat exchange tubes and the heat exchange tubes in the first group of heat exchange tubes are sequentially and alternately arranged in the circumferential direction.
As a further improvement of the above schemes, the distance m between adjacent heat exchange tubes on the same contour can be controlled to be 30-150 mm, and the distance n between adjacent heat exchange tubes on the same radial line is controlled to be 30-150 mm;
and the absolute value of m-n is 0 to 50 mm.
Preferably, m is 30-100 mm, and n is 30-100 mm.
For convenient maintenance, the synthesis gas collecting pipe can be formed by connecting the multistage barrel in a detachable mode in sequence, and a plurality of foot ladders are arranged on the inner side wall of the barrel at intervals in sequence along the axial direction.
Compared with the prior art, the isothermal shift reaction device provided by the invention has the advantages that the heat exchange tube is designed into the inner sleeve tube structure and the outer sleeve tube structure, so that the residence time and the sufficient heat removal of a refrigerant are ensured, the reaction temperature of a catalyst bed layer is accurately controlled, and the reaction effect is ensured. The optimized scheme can change the heat removal amount of the catalyst bed layer according to different reaction stages, so that the constant yield can be maintained in the whole process of the device operation and the whole active period of the catalyst without increasing the wall thickness of equipment.
Drawings
FIG. 1 is a schematic longitudinal cross-sectional view of an embodiment of the present invention;
FIG. 2 is a longitudinal cross-sectional view of a heat exchange tube in an embodiment of the present invention;
FIG. 3 is a view showing an assembly structure of a heat exchange tube and a tube box according to an embodiment of the present invention;
fig. 4 is a transverse sectional view along the arrangement of the heat exchange tubes in the present invention.
Detailed Description
The invention is described in further detail below with reference to the accompanying examples.
As shown in fig. 1 to 4, the isothermal shift reaction apparatus includes:
the furnace body is of a conventional structure and comprises an upper seal head 11, a lower seal head 12 and a cylinder body 13 connected between the upper seal head 11 and the lower seal head 12. The upper end enclosure 11 and the lower end enclosure are both provided with manholes 15, the upper end enclosure 11 is provided with a raw material gas inlet 14, the raw material gas inlet is connected with a gas distributor 16, and the raw material gas is uniformly dispersed into the space of the upper end enclosure through the gas distributor 16; the lower end enclosure is provided with a catalyst discharge port 18, and the bottom of the lower end enclosure 12 is provided with a synthesis gas outlet 17.
The catalyst frame 2 is used for filling a catalyst and is arranged in the cylinder 13. The catalyst frame 2 may be any one of the prior art as required, and may be an axial reactor, a radial reactor, or an axial-radial reactor, for example, which may be set as required. The reactor is a radial reactor, an upper port of a catalyst frame is closed, a gap is formed between the side wall of the catalyst frame and a cylinder, and a feed gas channel is formed in the gap; a plurality of air inlets (not shown in the figure) are arranged on the side wall of the catalyst frame at intervals and are communicated with the feed gas channel and the inner cavity of the catalyst frame. The raw material gas enters the catalyst frame from each air inlet on the side wall of the catalyst frame 2, and the through holes on the side wall of the catalyst frame play the role of a gas distributor.
The synthesis gas collecting pipe 3 is used for collecting synthesis gas and sending the synthesis gas out of the furnace body through a synthesis gas conveying pipeline, is arranged in the middle of the inner cavity of the catalyst frame, and is formed by sequentially and detachably connecting a plurality of sections of cylinders 31, and in the embodiment, the cylinders 31 are connected through flanges 34; the side wall of each cylinder 31 is provided with a plurality of air inlets (not shown in the figure) for the synthesis gas to enter the synthesis gas collecting pipe 3 from the catalyst bed layer; a plurality of footsteps 32 are sequentially arranged on the inner side wall of the cylinder 31 at intervals along the axial direction. The end cover is detachably connected to the upper end port of the synthesis gas collecting pipe 3, and is communicated with the manhole 15 after being disassembled, so that an overhaul worker can enter the synthesis gas collecting pipe 3; the lower port of the synthesis gas collecting pipe 3 is connected with a synthesis gas conveying pipeline. The synthesis gas delivery pipe is connected with the synthesis gas outlet 17 and is sent out through the synthesis gas outlet.
A plurality of heat exchange tubes 4, arranged longitudinally side by side in the catalyst bed space between the catalyst frame 2 and the synthesis gas collection tube 3. Each heat exchange tube 4 comprises an outer tube 41 and an inner tube 42, wherein one port of the outer tube 41 is closed by an upper port, a second port, i.e. a lower port, of the outer tube 41 is communicated with a steam collecting tank 51, and the steam collecting tank 51 is connected with an external steam drum (not shown in the figure) through a steam collecting pipeline 5.
The inner pipe 42 is inserted into the outer pipe 41 from the second port of the corresponding outer pipe 41, a gap is formed between the inner pipe 42 and the outer pipe 41, the first port, i.e., the upper port, of the inner pipe is communicated with the inner cavity of the outer pipe 41, and the second port, i.e., the lower port, of the inner pipe is communicated with the cooling water pipe. A spoiler 43 is provided in the cavity between the inner tube 42 and the outer tube 41. The spoiler 43 is spirally arranged in the axial direction of the inner pipe 42.
The heat exchange tubes 4 in this embodiment are divided into two groups, and correspondingly, there are two groups of cooling water tubes. Wherein the inlet of each inner tube in the first group of heat exchange tubes 4a is connected with the first cooling water pipeline 6a through a first cooling water ring pipe 61, and the inlet of each inner tube in the second group of heat exchange tubes 4b is connected with the second cooling water pipeline 6b through a second cooling water ring pipe 62; the two cooling water ring pipes play a role of redistribution, so that the cooling water sent from the outside uniformly enters each inner pipe connected with the cooling water ring pipes; a tube box may also be used or any of the prior art may be selected as desired. A valve (not shown in the figure) is arranged on the second cooling water pipeline 6 b; and the volume flow of the cooling water flowing through each inner tube in the first group of heat exchange tubes is 4-9 times of the volume flow of the cooling water flowing through each inner tube in the second group of heat exchange tubes.
There are various methods for controlling the flow of cooling water in the two groups of heat exchange tubes. Can be controlled by controlling the flow rate of cooling water entering the first cooling water pipeline and the second cooling water pipeline, and each heat exchange pipe in the first heat exchange pipes 4a is uniformly arranged on the cross section of the catalyst bed space; and all the heat exchange tubes in the second group of heat exchange tubes are uniformly arranged on the cross section of the catalyst bed layer space. The caliber of each inner tube in the first heat exchange tube is equal to that of each inner tube in the second group of heat exchange tubes, and the caliber of each outer tube in the first heat exchange tube is equal to that of each outer tube in the second group of heat exchange tubes.
Or the distribution of the cooling water flow in the two groups of heat exchange tubes can be realized by controlling the calibers of the two groups of heat exchange tubes. The heat exchange tubes in the first heat exchange tube 4a are still uniformly arranged on the cross section of the catalyst bed space; the heat exchange tubes in the second group of heat exchange tubes are uniformly arranged on the cross section of the catalyst bed layer space; however, the caliber of each inner tube in the first group of heat exchange tubes is 4-9 times of the caliber of each inner tube in the second group of heat exchange tubes, and the caliber of each outer tube in the first group of heat exchange tubes is 4-9 times of the caliber of each outer tube in the second group of heat exchange tubes. The flow rate is controlled by the caliber of the heat exchange tube.
And the distribution of cooling water flow in the two groups of heat exchange tubes can be realized through the arrangement of the heat exchange tubes. As shown in fig. 4, for the sake of easy identification, the heat exchange tubes 4 are radially arranged in the radial direction on the cross section of the catalyst bed space, and the heat exchange tubes are uniformly arranged in the circumferential direction on a plurality of concentric circumferential lines centering on the axis of the catalyst frame. The cross section of the catalyst bed layer space is divided into three areas from inside to outside, and only the heat exchange tubes in the first group of heat exchange tubes are arranged in a first area positioned on the inner side and a third area positioned on the outer side; the heat exchange tubes in the first group of heat exchange tubes and the heat exchange tubes in the second group of heat exchange tubes are simultaneously arranged in the second area in the middle, and the heat exchange tubes in the second group of heat exchange tubes and the heat exchange tubes in the first group of heat exchange tubes are sequentially and alternately arranged in the circumferential direction. In the embodiment, the distance m between adjacent heat exchange tubes on the same periphery is controlled to be 30-100 mm, and the distance n between adjacent heat exchange tubes on the same radial line is controlled to be 30-100 mm; and the absolute value of m-n is 0 to 50 mm.
Each of the cooling water pipeline and the steam collecting pipeline in the embodiment is connected with a steam drum (not shown in the figure). Other connection methods of the prior art can also be selected as required.
At the initial stage of operation of the device, the catalyst activity is high, the catalyst activity temperature is low, the heat that needs to be removed is many, the valve on the first cooling water pipeline is opened, and water is simultaneously fed into to two sets of heat exchange tubes.
The raw material gas enters the space above the catalyst frame from the raw material gas inlet through the gas distributor, enters the catalyst bed layer through the catalyst frame from each gas inlet through the raw material gas channel, and carries out shift reaction.
The cooling water entering the inner tubes of the two groups of heat exchange tubes ascends and overflows from the upper ports of the inner tubes, enters the gap between the inner tube and the outer tube, descends along the spoiler, and exchanges heat with the reaction heat generated by the catalyst bed layer to generate steam; enters the steam collecting box from the lower port of the outer pipe and is discharged from the steam collecting pipeline.
The two groups of heat exchange tubes work simultaneously, so that more heat is taken away, the catalyst bed layer is ensured to be maintained at a set temperature for conversion reaction, and the yield is constant at a set value.
In the later stage of the operation of the device, the activity temperature of the catalyst is increased due to the reduction of the activity of the catalyst; and a valve on the second cooling water pipeline 6b is closed, the second group of heat exchange tubes does not work, and only the first group of heat exchange tubes works. The working principle is the same as the above, but only one group of heat exchange tubes works, so that the heat exchange amount is reduced, the heat removal amount of a catalyst bed layer is reduced, the temperature of the catalyst bed layer is increased, the requirement of the activity temperature of the catalyst at the later stage is met, the shift reaction is normally carried out, and the yield is still maintained at the design value; and the steam pressure of the steam outlet drum is unchanged, and parameters of matched pipelines and equipment do not need to be changed.
Claims (9)
1. An isothermal shift reaction device comprises a furnace body and a catalyst frame (2) arranged in the furnace body, wherein a synthesis gas collecting pipe (3) is arranged in the middle of the catalyst frame (2), a gap is formed between the side wall of the catalyst frame and the side wall of the furnace body, and a plurality of air inlets communicated with the gap and the inner cavity of the catalyst frame are formed in the side wall of the catalyst frame; a plurality of heat exchange tubes (4) are arranged in a catalyst bed space between the catalyst frame (2) and the synthesis gas collecting tube (3), the heat exchange tubes (4) are longitudinally arranged in parallel in the catalyst bed space, inlets of the heat exchange tubes (4) are connected with a cooling water pipeline (6), and outlets of the heat exchange tubes are connected with a steam collecting pipeline (5);
the method is characterized in that:
the heat exchange tube (4) comprises an outer tube (41) and an inner tube (42), one port of the outer tube (41) is closed, and the second port of the outer tube (41) is communicated with the steam collecting pipeline (5);
the inner pipe (42) is inserted into the outer pipe (41) from a second port of the outer pipe (41), a gap is formed between the inner pipe (42) and the outer pipe (41), a first port of the inner pipe is communicated with an inner cavity of the outer pipe (41), and a second port of the inner pipe is communicated with the cooling water pipeline (6);
the heat exchange pipes (4) are divided into two groups, and correspondingly, the cooling water pipelines (6) are divided into two groups; the inlet of each inner pipe in the first group of heat exchange pipes (4a) is connected with a first cooling water pipeline (6a), and the inlet of each inner pipe in the second group of heat exchange pipes (4b) is connected with a second cooling water pipeline (6 b); a valve (61) is arranged on the second cooling water pipeline (6 b); controlling the volume flow of the refrigerant entering the first group of heat exchange tubes to be 4-9 times of the volume flow of the refrigerant entering the second group of heat exchange tubes;
the caliber of each inner tube in the first group of heat exchange tubes is 4-9 times that of each inner tube in the second group of heat exchange tubes, and the caliber of each outer tube in the first group of heat exchange tubes is 4-9 times that of each outer tube in the second group of heat exchange tubes.
2. Isothermal shift reactor according to claim 1, characterized in that a spoiler (43) is provided in the cavity between the inner tube (42) and the outer tube (41).
3. Isothermal shift reaction device according to claim 2, characterized in that said spoilers (43) are arranged spirally along the axial direction of said inner tube (42).
4. Isothermal shift reaction device according to claim 1, characterized in that each heat exchange tube of the first set of heat exchange tubes (4a) is arranged uniformly over the cross section of the catalyst bed space; and all the heat exchange tubes in the second group of heat exchange tubes are uniformly arranged on the cross section of the catalyst bed layer space.
5. Isothermal shift reaction device according to claim 1, characterized in that the heat exchange tubes (4) are arranged radially in the radial direction in the cross section of the catalyst bed space.
6. Isothermal shift reactor apparatus according to claim 5, characterized in that said heat exchange tubes are uniformly arranged on a plurality of concentric circumferential lines centered on the axis of said catalyst frame in the cross section of said catalyst bed space.
7. The isothermal shift reaction device according to claim 6, wherein the cross section of the catalyst bed space is divided into three regions from the inside to the outside, and only the heat exchange tubes of the first group of heat exchange tubes are arranged in the first region located at the inside and the third region located at the outside; the heat exchange tubes in the first group of heat exchange tubes and the heat exchange tubes in the second group of heat exchange tubes are simultaneously arranged in the second area in the middle, and the heat exchange tubes in the second group of heat exchange tubes and the heat exchange tubes in the first group of heat exchange tubes are sequentially and alternately arranged in the circumferential direction.
8. The isothermal shift reaction device according to any one of claims 5 to 7, wherein the distance m between adjacent heat exchange tubes on the same circumference is controlled to be 30 to 150mm, and the distance n between adjacent heat exchange tubes on the same radial line is controlled to be 30 to 150 mm;
and the absolute value of m-n is 0 to 50 mm.
9. The isothermal shift reaction device according to claim 8, wherein m is 30 to 100mm, and n is 30 to 100 mm.
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| CN110803681B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Gas-cooled transformation series isothermal transformation hydrogen production process matched with coal water slurry gasification and isothermal transformation furnace |
| CN110898768A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Double-isothermal-system conversion furnace |
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| CN104848712A (en) * | 2015-05-21 | 2015-08-19 | 陈永秋 | Line-up type full-contact heat exchange tube |
| CN204694122U (en) * | 2015-06-07 | 2015-10-07 | 大连理工大学 | A kind of a heatable brick bed road fume hot-water heat exchanger |
| WO2017063796A1 (en) * | 2015-10-16 | 2017-04-20 | Casale Sa | Isothermal tubular catalytic reactor |
| CN207881526U (en) * | 2018-01-26 | 2018-09-18 | 中信建筑设计研究总院有限公司 | A kind of shell-tube type vapor-water heat exchanger |
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