CN220803143U - Tube type fixed bed reactor - Google Patents
Tube type fixed bed reactor Download PDFInfo
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- CN220803143U CN220803143U CN202322650457.4U CN202322650457U CN220803143U CN 220803143 U CN220803143 U CN 220803143U CN 202322650457 U CN202322650457 U CN 202322650457U CN 220803143 U CN220803143 U CN 220803143U
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- 239000007788 liquid Substances 0.000 claims description 28
- 238000007789 sealing Methods 0.000 claims description 20
- 238000003491 array Methods 0.000 claims description 2
- HGINCPLSRVDWNT-UHFFFAOYSA-N Acrolein Chemical compound C=CC=O HGINCPLSRVDWNT-UHFFFAOYSA-N 0.000 abstract description 28
- 238000006243 chemical reaction Methods 0.000 abstract description 26
- AKXKFZDCRYJKTF-UHFFFAOYSA-N 3-Hydroxypropionaldehyde Chemical compound OCCC=O AKXKFZDCRYJKTF-UHFFFAOYSA-N 0.000 abstract description 14
- 239000003054 catalyst Substances 0.000 abstract description 9
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 8
- 238000006703 hydration reaction Methods 0.000 abstract description 7
- 239000012530 fluid Substances 0.000 description 22
- 238000002360 preparation method Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000012360 testing method Methods 0.000 description 5
- 230000036571 hydration Effects 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a shell and tube fixed bed reactor, which comprises a cylinder body (1), a hemispherical head (2), a spherical head (3), a shell and tube (4), a baffle plate (5), an upper tube plate (6) and a lower tube plate (7); the tubular fixed bed reactor is easy to process and manufacture, simple to operate and high in reaction efficiency. The tubular fixed bed reactor is easy to process and manufacture, simple to operate and high in reaction efficiency. When the tubular fixed bed reactor is used for preparing 3-hydroxy-propanal by acrolein hydration reaction, the conversion rate of acrolein reaches more than 85%, the selectivity of 3-hydroxy-propanal reaches more than 90%, and the loss rate of catalyst is less than 0.2%.
Description
[ Field of technology ]
The utility model belongs to the technical field of chemical equipment. More particularly, the present utility model relates to a shell and tube fixed bed reactor.
[ Background Art ]
The fixed bed catalytic reactor is a widely used reaction apparatus in chemical industry and petrochemical industry, and can be divided into adiabatic and non-adiabatic (tubular) type according to the heat exchange mode. For reactions with great thermal effects, yields are temperature sensitive and require high conversions and selectivities, heat must be removed or supplied with heat exchange medium to maintain the proper temperature, and tubular fixed bed reactors are very suitable.
At present, a considerable part of gas-solid phase catalytic reaction is carried out in a tubular fixed bed reactor, and the design and development technology of the reactor are mostly introduced from abroad, and the problem of large temperature difference exists in domestic devices generally, mainly due to uneven flow distribution of shell side coolant.
In order to solve some technical defects existing in the prior art, the inventor finally completes the utility model through a great deal of experimental research and analysis summary.
[ utility model ]
[ Problem to be solved ]
The utility model aims to provide a tubular fixed bed reactor.
Technical scheme
The utility model is realized by the following technical scheme.
The utility model relates to a shell and tube fixed bed reactor, which comprises a cylinder body 1, and further comprises a hemispherical sealing head 2, a spherical sealing head 3, a shell and tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to a preferred embodiment of the utility model, the ratio of diameter to height of the cylinder 1 is 1:2.0 to 5.0.
According to another preferred embodiment of the utility model, the ratio of the diameter of the tubulation 4 to the inner diameter of the cylinder 1 is 1: 30-50.
According to another preferred embodiment of the utility model, the ratio of the diameter to the height of the tubulation 4 is 1:20 to 80, the ratio of the diameter of the tubulation 4 to the spacing between tubulations 4 is 1:0.5 to 2.0.
According to another preferred embodiment of the utility model, the diameter of the baffle 5 is the same as the inner diameter of the cylinder 1, or the ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is 0.80-0.95: 1.
According to another preferred embodiment of the utility model, the ratio of the height of the tubes 4 to the spacing of the baffles 5 from each other is 1:0.10 to 0.25.
According to another preferred embodiment of the utility model, the maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 300-600 mm.
According to another preferred embodiment of the utility model, the ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1: 100-200.
According to another preferred embodiment of the utility model, the ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:3 to 5.
According to another preferred embodiment of the utility model, the ratio of the height of the spherical head 3 to the height of the cylinder 1 is 1:4 to 6.
The present utility model will be described in detail below.
The utility model relates to a tubular fixed bed reactor, the specific structure of which is shown in figure 1.
The tube type fixed bed reactor comprises a cylinder body 1, and also comprises a hemispherical sealing head 2, a spherical sealing head 3, a tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to the utility model, the ratio of diameter to height of the cylinder 1 is 1:2.0 to 5.0. If the ratio of the diameter to the height of the cylinder 1 is greater than 1:2.0, the heat transfer efficiency of the tubulation is affected, thereby affecting the reaction efficiency; if the ratio of the diameter to the height of the cylinder 1 is less than 1:5.0, the processing difficulty of the equipment is increased; thus, the ratio of diameter to height of the cylinder 1 is 1:2.0 to 5.0 are suitable, preferably 1:2.6 to 4.5;
The main function of the tube array 4 in the tube array fixed bed reactor according to the utility model is to charge the catalyst used for the reaction.
The ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1: 30-50. If the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is greater than 1:30, the diameter of the tube array is too large, which is not beneficial to the removal of reaction heat and affects the reaction efficiency; if the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is less than 1:50, the diameter of the tube array is too small, and the number of tube arrays required by the same catalyst loading capacity is large, so that the manufacturing difficulty of equipment is increased; thus, the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1:30 to 50 are reasonable, preferably 1: 35-45;
The ratio of the diameter to the height of the tube array 4 is 1:20 to 80 percent. If the ratio of the diameter to the height of the tube array 4 is greater than 1:20, the mixing degree of the fluid in the tube array is poor, the diffusion speed of the reactant is low, and the reaction efficiency is low; if the ratio of the diameter to the height of the tube array 4 is less than 1:80, which can lead to imbalance in the internal fluid pressure of the reactor, thereby affecting the uniformity of the reaction; thus, the ratio of the diameter to the height of the tube array 4 is 1:20 to 80 are suitable, preferably 1:30 to 68, more preferably 1: 36-60;
The ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:0.5 to 2.0. If the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is greater than 1:0.5, the heat transfer efficiency of the tube array is low, and the reaction efficiency is affected; if the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is less than 1:2.0, the reaction efficiency is not obviously improved, but the manufacturing cost of equipment is increased, so that the method is uneconomical; thus, the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:0.5 to 2.0 are suitable, preferably 1:0.8 to 1.6;
The baffle plate 5 used in the present utility model is a parallel baffle plate which can increase the flow rate of fluid (circulating liquid) in the cylinder, force the fluid to be deflected a plurality of times according to a prescribed path and is arranged on the inner wall of the shell.
According to the utility model, the diameter of the baffle 5 is the same as the inner diameter of the cylinder 1, or the ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is 0.80-0.95: 1. when the diameter of the baffle plate 5 is the same as or different from the inner diameter of the cylinder body 1, the baffle plate 5 has a straight edge. The maximum distance between the straight edge of the baffle plate 5 and the inner wall of the cylinder body 1 is 300-600 mm. If the maximum distance between the straight edge of the baffle plate 5 and the inner wall of the cylinder body 1 is smaller than 300mm, the flow resistance of circulating liquid is increased, and the tubulation is easy to vibrate and destroy; if the maximum distance between the straight edge of the baffle plate 5 and the inner wall of the cylinder body 1 is more than 600mm, the liquid of the circulating liquid part is easy to stagnate, and a dead zone which is unfavorable for heat transfer is formed; it is therefore appropriate that the maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 300-600 mm, preferably 360-420 mm;
When the diameter of the baffle plate 5 is different from the inner diameter of the cylinder body 1, the ratio of the diameter of the baffle plate 5 to the inner diameter of the cylinder body 1 is 0.80-0.95: 1. if the ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is less than 0.80:1, partial liquid flow of the circulating liquid is easy to be uneven, which is not beneficial to the transfer of reaction heat; if the ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is greater than 0.95:1, the flowing resistance of the circulating liquid is increased, and equipment is easy to damage; thus, the ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is between 0.80 and 0.95:1 is preferably 0.83 to 0.92:1, a step of;
According to the utility model, the ratio of the height of the tubes 4 to the distance between the baffles 5 is 1:0.10 to 0.25. If the ratio of the height of the tube array 4 to the distance between the baffles 5 is greater than 1:0.10, the number of baffle plates is large, the reaction effect of the reactor is not obviously improved, the manufacturing cost of equipment is increased, and the method is uneconomical; if the ratio of the height of the tube array 4 to the distance between the baffles 5 is less than 1:0.25, the number of baffle plates is small, and the circulating effect of the circulating liquid is affected, so that the reaction efficiency is affected; thus, the ratio of the height of the tube array 4 to the spacing of the baffles 5 from each other is 1:0.10 to 0.25 is reasonable, preferably 1:0.13 to 0.22;
In the present utility model, the ratio of the thickness of the baffle 5 to the spacing of the baffles 5 from each other is 1: 100-200. If the ratio of the thickness of the baffle 5 to the spacing of the baffles 5 from each other is greater than 1:100, the baffle plate has large thickness, the double-flow effect is not influenced, the equipment investment is increased, and the method is uneconomical; if the ratio of the thickness of the baffle 5 to the spacing of the baffles 5 from each other is less than 1:200, the thickness of the baffle plate is small, and the circulating liquid can cause deformation of the baffle plate due to circulating flow, so that equipment is damaged; thus, the ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1:100 to 200 are suitable, preferably 1:120 to 180, more preferably 1: 132-165;
In the utility model, the ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:3 to 5. If the ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is greater than 1:3, the welding of the sealing head and the cylinder body is not facilitated, and the manufacturing difficulty of the equipment is increased; if the ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is less than 1:5, the resistance of the materials in the using process of the reactor is larger, which is unfavorable for the reaction; therefore, the ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:3 to 5 are appropriate;
the ratio of the height of the spherical sealing head 3 to the height of the cylinder body 1 is 1:4 to 6. If the ratio of the height of the spherical head 3 to the height of the cylinder 1 is greater than 1:4, the welding of the sealing head and the cylinder body is not facilitated, and the manufacturing difficulty of the equipment is increased; if the ratio of the height of the spherical head 3 to the height of the cylinder 1 is less than 1:6, the resistance of the materials in the using process of the reactor is larger, which is unfavorable for the reaction; therefore, the ratio of the height of the spherical head 3 to the height of the cylinder 1 is 1:4 to 6 are preferable.
According to the preparation method described in CN110204422B, 3-hydroxy-propanal is prepared by the hydration reaction of acrolein by using the tubular fixed bed reactor of the utility model. The preparation test result shows that when the tubular fixed bed reactor is used, the conversion rate of acrolein reaches more than 85%, the selectivity of 3-hydroxy propanal reaches more than 90%, and the catalyst loss rate is less than 0.2%.
[ Advantageous effects ]
The beneficial effects of the utility model are as follows: the tubular fixed bed reactor is easy to process and manufacture, simple to operate and high in reaction efficiency. When the tubular fixed bed reactor is used for preparing 3-hydroxy-propanal by acrolein hydration reaction, the conversion rate of acrolein reaches more than 85%, the selectivity of 3-hydroxy-propanal reaches more than 90%, and the loss rate of catalyst is less than 0.2%.
[ Description of the drawings ]
FIG. 1 is a front view of a tubular fixed bed reactor of the present utility model;
In the figure:
1-a cylinder; 11-a circulating liquid inlet; 12-a circulating liquid outlet; 13-a first level gauge mounting port; 14-a second level gauge mounting port; 15-a first thermometer mounting port; 2-hemispherical closure heads; 21-a feed inlet; 22-pressure gauge mounting port; 23-a safety valve mounting port; 3-spherical end socket; 31-a discharge hole; 32-a second thermometer mounting port; 4-tube array; 5-baffle plate; 6-an upper tube plate; 7-lower tube plate.
[ Detailed description ] of the invention
The utility model will be better understood by the following examples.
Example 1: the utility model relates to a tubular fixed bed reactor
The implementation of this example is as follows:
The shell-and-tube fixed bed reactor comprises a cylinder body 1, a hemispherical head 2, a spherical head 3, a shell-and-tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
wherein, the ratio of the diameter to the height of the cylinder 1 is 1:4.0. the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1:44. the ratio of the diameter to the height of the tube array 4 is 1:60, the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:1.0.
The diameter of the baffle 5 is the same as the inner diameter of the cylinder 1. The maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 400mm. The ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1:200.
The ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:3. the ratio of the height of the spherical sealing head 3 to the height of the cylinder body 1 is 1:5.
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to the preparation method described in CN110204422B, 3-hydroxypropionaldehyde was prepared by acrolein hydration using the tubular fixed bed reactor described in this example, and the result of the test was that the conversion of acrolein was 85.5%, the selectivity for 3-hydroxypropionaldehyde was 90.3%, and the loss rate of catalyst was 0.18%.
Example 2: the utility model relates to a tubular fixed bed reactor
The implementation of this example is as follows:
The shell-and-tube fixed bed reactor comprises a cylinder body 1, a hemispherical head 2, a spherical head 3, a shell-and-tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
Wherein, the ratio of the diameter to the height of the cylinder 1 is 1:2.0. the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1:50. the ratio of the diameter to the height of the tube array 4 is 1:20, the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:2.0.
The diameter of the baffle 5 is the same as the inner diameter of the cylinder 1. The maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 300mm. The ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1:170.
The ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:4. the ratio of the height of the spherical sealing head 3 to the height of the cylinder body 1 is 1:4.
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to the preparation method described in CN110204422B, 3-hydroxypropionaldehyde was prepared by acrolein hydration using the tubular fixed bed reactor described in this example, and the result of the test was that the conversion of acrolein was 88.2%, the selectivity for 3-hydroxypropionaldehyde was 92.8%, and the loss rate of catalyst was 0.19%.
Example 3: the utility model relates to a tubular fixed bed reactor
The implementation of this example is as follows:
The shell-and-tube fixed bed reactor comprises a cylinder body 1, a hemispherical head 2, a spherical head 3, a shell-and-tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
Wherein, the ratio of the diameter to the height of the cylinder 1 is 1:5.0. the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1:30. the ratio of the diameter to the height of the tube array 4 is 1:40, the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:1.5.
The ratio of the diameter of the baffle 5 to the inner diameter of the cylinder 1 is 0.80:1. the maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 600mm. The ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1:100.
The ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:5. the ratio of the height of the spherical sealing head 3 to the height of the cylinder body 1 is 1:6.
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to the preparation method described in CN110204422B, 3-hydroxypropionaldehyde was prepared by acrolein hydration using the tubular fixed bed reactor described in this example, and the result of the test was that the conversion of acrolein was 86.4%, the selectivity for 3-hydroxypropionaldehyde was 91.2%, and the loss rate of catalyst was 0.18%.
Example 4: the utility model relates to a tubular fixed bed reactor
The implementation of this example is as follows:
The shell-and-tube fixed bed reactor comprises a cylinder body 1, a hemispherical head 2, a spherical head 3, a shell-and-tube 4, a baffle plate 5, an upper tube plate 6 and a lower tube plate 7; an upper tube plate 6 is fixedly arranged at the upper end of the cylinder body 1, the upper tube plate 6 is connected with the hemispherical head 2, a lower tube plate 7 is fixedly arranged at the lower end of the cylinder body 1, the lower tube plate 7 is connected with the spherical head 3, the tubes 4 are uniformly arranged in the cylinder body 1 in a manner parallel to the central axis of the cylinder body 1, and the baffle plates 5 are staggered in a manner perpendicular to the central axis of the cylinder body 1;
Wherein, the ratio of the diameter to the height of the cylinder 1 is 1:3.0. the ratio of the diameter of the tube array 4 to the inner diameter of the cylinder 1 is 1:36. the ratio of the diameter to the height of the tube array 4 is 1:80, the ratio of the diameter of the tubulars 4 to the spacing between tubulars 4 is 1:0.5.
The ratio of the diameter of baffle 5 to the inner diameter of cylinder 1 is 0.95:1. the maximum distance between the straight edge of the baffle 5 and the inner wall of the cylinder 1 is 500mm. The ratio of the thickness of the baffles 5 to the spacing of the baffles 5 from each other is 1:130.
The ratio of the height of the hemispherical head 2 to the height of the cylinder 1 is 1:4. the ratio of the height of the spherical sealing head 3 to the height of the cylinder body 1 is 1:5.
A feed port 21 is arranged in the center of the upper end of the hemispherical head 2, a pressure gauge mounting port 22 is arranged on one side of the feed port 21, and a safety valve mounting port 23 is arranged on the other side of the feed port 21; a first liquid level meter mounting port 13 and a second liquid level meter mounting port 14 are arranged on one side of the straight barrel part of the hemispherical head 2, and a first thermometer mounting port 15 is arranged on the other side; a discharge hole 31 is formed in the center of the lower end of the spherical sealing head 3, and a second thermometer mounting hole 32 is formed in one side of the discharge hole 31;
A circulating fluid inlet 11 is arranged at the lower part of the cylinder body 1, and a circulating fluid outlet 12 is arranged at the upper part of the cylinder body 1 at the side opposite to the circulating fluid inlet 11.
According to the preparation method described in CN110204422B, 3-hydroxypropionaldehyde was prepared by acrolein hydration using the tubular fixed bed reactor described in this example, and the result of the test was that the conversion of acrolein was 87.5%, the selectivity for 3-hydroxypropionaldehyde was 93.0%, and the catalyst loss was 0.16%.
Claims (10)
1. The shell and tube fixed bed reactor comprises a cylinder body (1) and is characterized by also comprising a hemispherical sealing head (2), a spherical sealing head (3), a shell and tube (4), a baffle plate (5), an upper tube plate (6) and a lower tube plate (7); an upper tube plate (6) is fixedly arranged at the upper end of the cylinder body (1), the upper tube plate (6) is connected with the hemispherical head (2), a lower tube plate (7) is fixedly arranged at the lower end of the cylinder body (1), the lower tube plate (7) is connected with the spherical head (3), the tubes (4) are uniformly arranged in the cylinder body (1) in a mode of being parallel to the central axis of the cylinder body (1), and baffle plates (5) are arranged in a staggered mode in a mode of being perpendicular to the central axis of the cylinder body (1);
A feed inlet (21) is arranged in the center of the upper end of the hemispherical head (2), a pressure gauge mounting port (22) is arranged on one side of the feed inlet (21), and a safety valve mounting port (23) is arranged on the other side of the feed inlet; a first liquid level meter mounting port (13) and a second liquid level meter mounting port (14) are arranged on one side of a straight cylinder part of the hemispherical head (2), and a first thermometer mounting port (15) is arranged on the other side of the straight cylinder part; a discharge hole (31) is formed in the center of the lower end of the spherical sealing head (3), and a second thermometer mounting hole (32) is formed in one side of the discharge hole (31);
The lower part of the cylinder body (1) is provided with a circulating liquid inlet (11), and the upper part of the cylinder body (1) is provided with a circulating liquid outlet (12) at one side opposite to the circulating liquid inlet (11).
2. Tubular fixed bed reactor according to claim 1, characterized in that the ratio of diameter to height of the cylinder (1) is 1:2.0 to 5.0.
3. The shell-and-tube fixed bed reactor according to claim 1, characterized in that the ratio of the diameter of the shell-and-tube (4) to the inner diameter of the cylinder (1) is 1: 30-50.
4. Tubular fixed bed reactor according to claim 1, characterized in that the ratio of the diameter to the height of the tubular (4) is 1:20 to 80, the ratio of the diameter of the tube array (4) to the spacing between the tube arrays (4) is 1:0.5 to 2.0.
5. The shell-and-tube fixed bed reactor according to claim 1, characterized in that the diameter of the baffle (5) is the same as the inner diameter of the cylinder (1) or the ratio of the diameter of the baffle (5) to the inner diameter of the cylinder (1) is 0.80-0.95: 1.
6. The shell-and-tube fixed bed reactor according to claim 1, characterized in that the ratio of the height of the tubes (4) to the spacing of the baffles (5) from each other is 1:0.10 to 0.25.
7. The tube array type fixed bed reactor as claimed in claim 1, wherein the maximum distance between the straight edge of the baffle plate (5) and the inner wall of the cylinder (1) is 300-600 mm.
8. The shell-and-tube fixed bed reactor according to claim 1, characterized in that the ratio of the thickness of the baffles (5) to the spacing of the baffles (5) from each other is 1: 100-200.
9. The shell-and-tube fixed bed reactor according to claim 1, characterized in that the ratio of the height of the hemispherical head (2) to the height of the cylinder (1) is 1:3 to 5.
10. Tubular fixed bed reactor according to claim 1, characterized in that the ratio of the height of the spherical head (3) to the height of the cylinder (1) is 1:4 to 6.
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| CN202322650457.4U CN220803143U (en) | 2023-09-28 | 2023-09-28 | Tube type fixed bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202322650457.4U CN220803143U (en) | 2023-09-28 | 2023-09-28 | Tube type fixed bed reactor |
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