CN116037006A - Tube array type gas-liquid homogeneous reactor - Google Patents
Tube array type gas-liquid homogeneous reactor Download PDFInfo
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- CN116037006A CN116037006A CN202211729791.2A CN202211729791A CN116037006A CN 116037006 A CN116037006 A CN 116037006A CN 202211729791 A CN202211729791 A CN 202211729791A CN 116037006 A CN116037006 A CN 116037006A
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- 239000007788 liquid Substances 0.000 title claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 92
- 238000009826 distribution Methods 0.000 claims abstract description 58
- 239000007791 liquid phase Substances 0.000 claims abstract description 45
- 239000012071 phase Substances 0.000 claims abstract description 34
- 238000007789 sealing Methods 0.000 claims abstract description 14
- 239000002184 metal Substances 0.000 claims description 4
- -1 polytetrafluoroethylene Polymers 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 2
- 238000005245 sintering Methods 0.000 claims 2
- 239000000463 material Substances 0.000 abstract description 55
- AMIMRNSIRUDHCM-UHFFFAOYSA-N Isopropylaldehyde Chemical compound CC(C)C=O AMIMRNSIRUDHCM-UHFFFAOYSA-N 0.000 description 18
- 239000007795 chemical reaction product Substances 0.000 description 12
- 239000007789 gas Substances 0.000 description 12
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 9
- 239000000047 product Substances 0.000 description 8
- 239000011949 solid catalyst Substances 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- FALRKNHUBBKYCC-UHFFFAOYSA-N 2-(chloromethyl)pyridine-3-carbonitrile Chemical compound ClCC1=NC=CC=C1C#N FALRKNHUBBKYCC-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000010574 gas phase reaction Methods 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 229940014800 succinic anhydride Drugs 0.000 description 3
- 238000009827 uniform distribution Methods 0.000 description 3
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 2
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052573 porcelain Inorganic materials 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 238000004891 communication Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00548—Flow
-
- 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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00831—Stationary elements
- B01J2208/0084—Stationary elements inside the bed, e.g. baffles
-
- 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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a tubular gas-liquid homogeneous reactor which comprises an upper sealing head, a reaction section, a homogeneous distribution section and a lower sealing head, wherein the upper sealing head is provided with a discharge hole, the lower sealing head is provided with a liquid phase feed inlet, the reaction section is provided with a plurality of reaction tubulations, the homogeneous distribution section is provided with a plurality of micron-sized distribution pipes, the micron-sized distribution pipes are communicated with the reaction tubulations in a one-to-one correspondence manner, and the side wall of the homogeneous distribution section between a middle tube plate and a lower tube plate is provided with a gas phase feed inlet. The tubular gas-liquid homogeneous reactor solves the problem that gas-phase materials cannot be uniformly mixed with liquid-phase materials in all the tubes of the reactor by arranging the homogeneous distribution sections, can realize the sufficient contact flow of the gas-phase materials and the liquid-phase materials in all the tubes in approximately equal proportion, does not have the phenomena of gas resistance, bias flow, bubble flow and the like which damage the reaction, and improves the conversion rate of the liquid-phase materials by uniformly mixing the gas-phase materials and the liquid-phase materials in all the tubes.
Description
Technical Field
The invention belongs to the field of reactors, and particularly relates to a tubular gas-liquid homogeneous reactor.
Background
The existing reaction (such as hydrogenation reaction, oxidation reaction, oxo aldehyde hydrogenation reaction and the like) of liquid-phase materials and gas-phase materials is difficult to form uniform distribution with the liquid-phase materials in all tubes of a reactor because the gas-phase materials are easily subjected to external environmental factors such as resistance, temperature, flow forms and the like to form irregular dispersion characteristics, so that the reaction effect in different tubes of the same reactor is quite different, hot spots and heavy component generation are easy to form, the raw material conversion rate and the selectivity of target products are influenced, the overall reaction effect is not ideal, and only measures of reacting the gas-phase materials with the gas-phase materials can be adopted to solve the problems.
At this time, the liquid phase materials need to be gasified into gas phase materials, which not only greatly increases energy consumption, but also generally reduces the volume space velocity of the catalyst (calculated by reaction raw materials) in the gas phase reaction, which results in much higher loading of the catalyst and the volume of the reactor than in the liquid phase reaction, increases more investment cost, and limits processing capacity. Meanwhile, part of liquid materials cannot be gasified under the corresponding reaction temperature and pressure, so that a fixed bed large circulation ratio reaction system is forced to be adopted, and the operation investment is high and the energy consumption is high.
The conventional micron-sized distribution pipes are generally internally provided with gas-phase materials, liquid-phase materials are arranged outside the pipes, a single distribution pipe is generally arranged at a place where the micron-sized distribution pipes are used, the gas-phase materials are diffused into the liquid-phase materials outside the pipes from the inside of the pipes, the distribution mode is often used for a butyraldehyde oxidation reactor, the distribution mode is uniformly distributed in the surface area of the distribution pipe, and large bubbles are easily formed in other liquid-phase material areas far away from the distribution pipe again, so that the reaction effect is poor.
How to adopt effective means to realize the uniform distribution of liquid phase materials and gas phase materials in all the tubes of the reactor is a technical difficulty to be solved in the field.
Disclosure of Invention
In view of the above, the present invention aims to provide a tubular gas-liquid homogeneous reactor, so as to promote the uniform mixing of gas phase materials and liquid phase materials, improve the conversion rate of the liquid phase materials, and reduce the volume of the reactor.
In order to achieve the above purpose, the technical scheme of the invention is realized as follows:
a tubular gas-liquid homogeneous reactor comprises an upper end enclosure, a reaction section, a homogeneous distribution section and a lower end enclosure which are sequentially communicated from top to bottom, wherein the upper end of the upper end enclosure is provided with a discharge hole, the lower end of the lower end enclosure is provided with a liquid phase feed inlet,
the upper end of the reaction section is fixedly connected with an upper tube plate, a middle tube plate is fixedly connected between the reaction section and the homogeneous distribution section, the lower end of the homogeneous distribution section is fixedly connected with a lower tube plate, a plurality of reaction tubes are arranged between the upper tube plate and the middle tube plate, the upper ends of the reaction tubes are communicated with the upper end of the upper tube plate, a plurality of micron-sized distribution tubes are arranged between the middle tube plate and the lower tube plate, the upper ends of the micron-sized distribution tubes are communicated with the lower ends of the reaction tubes in a one-to-one correspondence manner, the communication modes comprise, but are not limited to, threaded connection, welding, flange connection and the like, the lower ends of the micron-sized distribution tubes are communicated with the lower tube plate, the side wall of the homogeneous distribution section between the middle tube plate and the lower tube plate is provided with a gas-phase feed inlet, liquid-phase materials enter the reactor from the liquid-phase feed inlet, enter the micron-sized distribution tubes from the gas-phase feed inlet, enter the reactor from the gas-phase feed inlet, uniformly mix with the liquid-phase materials through micropores on the side wall of the micron-sized distribution tubes in the homogeneous distribution section, jointly enter the reaction tubes upwards, the micron-phase materials are filled with the catalyst, under the action of the catalyst, the reaction tubes, the liquid-phase materials react with the gas-phase materials, and the liquid-phase materials are discharged from the upper tube through the upper end.
The inventive concept of the present application is: by arranging the homogeneous distribution section before the reaction section and using a certain number of micron-sized distribution pipes, the micron-sized form of the gas-phase material is mixed with the liquid-phase material, the time for reaching the catalyst bed after the formation of the micro-bubbles is shortened, the formation and distribution effects of the micro-bubbles are fully ensured, and the interphase area is increased. Meanwhile, the number of the micrometer-level separation tubes is the same as that of the reaction tubes, so that the proportion of gas-phase materials and liquid-phase materials in each reaction tube is ensured to be highly consistent, and the key requirement of uniform distribution of the gas-phase materials and the liquid-phase materials is met. Meanwhile, the circulation quantity and the reaction pressure of gas-phase reaction materials are reduced, the formation of reaction hot spots is avoided, the raw material conversion rate and the selectivity of target products are improved, the reaction space velocity is also improved, and the loading quantity of the catalyst and the manufacturing cost of the reactor are reduced.
Further, the outer diameter of the reaction tube array is 10-150 mm, the wall thickness is 1-8 mm, the length is 500-20000 mm, and the number is 6-10000.
Further, a spring support is arranged in the reaction tube, when the catalyst in the reaction tube is a solid catalyst, the spring support can play a role in supporting, compared with an inert porcelain ball, the spring support can play a role in preventing vortex of materials, which is not provided with the porcelain ball, and when the reaction tube is a liquid-phase catalyst, the spring support does not need to be arranged; preferably, the height of the spring support is 50-500 mm.
Further, the outer diameter of the micrometer-sized fraction tube is 10-150 mm, the wall thickness is 1-8 mm, the length is 100-5000 mm, the aperture is 5-1000 μm, and the number is 6-10000.
Further, a heat exchange medium inlet is arranged on the side wall of the lower end of the reaction section between the upper tube plate and the middle tube plate, a heat exchange medium outlet is arranged at the upper end of the reaction section, the heat exchange medium enters the reaction section from the heat exchange medium inlet and is discharged from the heat exchange medium outlet, heat is taken by the heat exchange medium for exothermic reaction, heat is supplied by the heat exchange medium for endothermic reaction, and the reaction temperature is flexibly controlled.
Further, the device also comprises a thermometer, wherein the thermometer is fixedly connected with the upper end socket, the lower end of the thermometer penetrates through the upper end socket and stretches into the reaction tube nest, and the thermometer is used for monitoring whether the temperature in the reaction tube nest is in a proper range.
Further, the working pressure of the tubular gas-liquid homogeneous phase reactor is-0.1 to 20MPaG, and the working temperature is-20 to 600 ℃.
Further, the micrometer-sized fraction tube includes, but is not limited to, one of a metal sintered tube, a wire mesh sintered tube, a polytetrafluoroethylene microporous tube, a ceramic microporous tube.
Compared with the prior art, the tubular gas-liquid homogeneous reactor has the following advantages:
(1) The tube array type gas-liquid homogeneous reactor solves the problem that gas phase materials cannot be uniformly mixed with liquid phase materials in all tubes of the reactor by arranging the homogeneous distribution sections, can realize that the gas phase materials and the liquid phase materials fully contact and flow in the tubes in approximately equal proportion, does not have the phenomena of gas resistance, bias flow, bubble flow and the like which damage reaction, and ensures that the gas phase materials and the liquid phase materials are uniformly mixed in each tube array, so that the conversion rate of the liquid phase materials is improved by 10% -500%;
(2) The shell-and-tube gas-liquid homogeneous reactor can participate in the reaction without gasifying liquid phase materials into gas phase materials, the volumes of the catalyst and the reactor can be correspondingly reduced, and the size of the reactor for the gas phase reaction is phi 2000 multiplied by 16000mm by taking 5 ten thousand tons/year acetone hydrogenation for producing isopropanol as an example, and after the reactor is adopted, the size of the reactor for the liquid phase reaction is phi 1000 multiplied by 9000mm, the volume of the reactor is reduced by about 86 percent, and the investment and the occupied area are saved.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention. In the drawings:
FIG. 1 is a schematic structural diagram of a tubular gas-liquid homogeneous reactor according to an embodiment of the present invention;
fig. 2 is a schematic diagram of the material distribution and flow direction of a micrometer scale distribution pipe according to an embodiment of the present invention.
Reference numerals illustrate:
1. an upper end enclosure; 2. a reaction section; 3. a reaction tube array; 4. a spring support; 5. a middle tube plate; 6. a homogeneously distributed section; 7. a micrometer-sized fraction tube; 8. a lower end enclosure; 9. a thermometer; 10. an upper tube sheet; 11. a lower tube sheet; 12. and (3) a flange.
Detailed Description
It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
The invention will be described in detail below with reference to the drawings in connection with embodiments.
The invention relates to a tubular gas-liquid homogeneous reactor, which comprises an upper end enclosure 1, a reaction section 2, a homogeneous distribution section 6 and a lower end enclosure 8 which are sequentially communicated from top to bottom, wherein the upper end enclosure 1, the reaction section 2 and the homogeneous distribution section 6 are all welded, the homogeneous distribution section 6 is connected with the lower end enclosure 8 through a flange 12, the upper end of the upper end enclosure 1 is provided with a discharge port, the lower end of the lower end enclosure 8 is provided with a liquid phase feed port, the tubular gas-liquid homogeneous reactor also comprises a thermometer 9, the thermometer 9 is fixedly connected with the upper end enclosure 1, the lower end of the thermometer 9 penetrates through the upper end enclosure 1 and stretches into a reaction tubular 3,
an upper tube plate 10 is fixedly connected to the upper end of the reaction section 2, a middle tube plate 5 is fixedly connected between the reaction section 2 and the homogeneous distribution section 6, a lower tube plate 11 is fixedly connected to the lower end of the homogeneous distribution section 6, a plurality of reaction tubes 3 are arranged between the upper tube plate 10 and the middle tube plate 5, the upper ends of the reaction tubes 3 are communicated with the upper end socket 1, a plurality of micro-scale distribution tubes 7 are arranged between the middle tube plate 5 and the lower tube plate 11, the micro-scale distribution tubes 7 are metal sintered tubes, the upper ends of the micro-scale distribution tubes 7 are communicated with the lower ends of the reaction tubes 3 in a one-to-one correspondence manner, the lower ends of the micro-scale distribution tubes 7 are communicated with the lower end socket 8 in a welding manner, gas phase feed inlets are arranged on the side wall of the homogeneous distribution section 6 between the middle tube plate 5 and the lower tube plate 11,
the outer diameter of the reaction tube array 3 is 10-150 mm, the wall thickness is 1-8 mm, the length is 500-20000 mm, and the number is 6-10000.
The reaction tube array 3 is internally provided with a spring support 4, and the height of the spring support 4 is 50-500 mm.
The outer diameter of the micrometer-sized fraction tube 7 is 10-150 mm, the wall thickness is 1-8 mm, the length is 100-5000 mm, the aperture is 5-1000 μm, and the number is 6-10000.
The side wall of the lower end of the reaction section 2 between the upper tube plate 10 and the middle tube plate 5 is provided with a heat exchange medium inlet, the upper end is provided with a heat exchange medium outlet, and the heat exchange medium enters the reaction section 2 from the heat exchange medium inlet and is discharged from the heat exchange medium outlet.
Example 1
(1) Maleic anhydride solution (the concentration of maleic anhydride is 3% -30% and the balance succinic anhydride) is sent to a liquid-phase feed inlet at the bottom of a lower seal head 8 of the reactor through an external pump, hydrogen is sent to a gas-phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The maleic anhydride solution feed rate was controlled to 5.0t/h and the hydrogen gas feed rate was controlled to 20Nm 3 And/h, controlling the flow rate of the liquid phase material in the reaction tube array 3 to be 0.8m/s, controlling the reaction pressure to be 1.0MPaG, controlling the outlet pressure of the hydrogen compressor to be 1.5MPaG, wherein the internal and external pressure difference of the micrometer level distribution tube 7 is about 0.5MPaG, and enabling the reaction product to flow out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of the raw maleic anhydride was about 98.0%, and the product yield was about 97.1%.
Example 2
(1) Maleic anhydride solution (the concentration of maleic anhydride is 3% -30% and the balance succinic anhydride) is sent to a liquid-phase feed inlet at the bottom of a lower seal head 8 of the reactor through an external pump, hydrogen is sent to a gas-phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The maleic anhydride solution feed rate was controlled to 5.0t/h and the hydrogen gas feed rate was controlled to 20Nm 3 And/h, controlling the flow rate of the liquid phase material in the reaction tube array 3 to be 0.8m/s, controlling the reaction pressure to be 1.0MPaG, controlling the outlet pressure of the hydrogen compressor to be 2.0MPaG, wherein the internal and external pressure difference of the micrometer level distribution tube 7 is about 1.0MPaG, and enabling the reaction product to flow out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of the raw maleic anhydride was about 98.7%, and the product yield was about 97.9%.
Example 3
(1) Maleic anhydride solution (the concentration of maleic anhydride is 3% -30% and the balance succinic anhydride) is sent to a liquid-phase feed inlet at the bottom of a lower seal head 8 of the reactor through an external pump, hydrogen is sent to a gas-phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The maleic anhydride solution feed rate was controlled to 5.0t/h and the hydrogen gas feed rate was controlled to 20Nm 3 And/h, controlling the flow rate of the liquid phase material in the tube array to be 0.8m/s, controlling the reaction pressure to be 1.0MPaG, controlling the outlet pressure of the hydrogen compressor to be 3.0MPaG, and at the moment, the internal and external pressure difference of the micrometer level distribution tube 7 is about 2.0MPaG, and enabling the reaction product to flow out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of the raw maleic anhydride was about 99.7%, and the product yield was about 99.1%.
Example 4
(1) The isobutyraldehyde is sent to a liquid phase feed inlet at the bottom of a reactor lower seal head 8 through an external pump, air is sent to a gas phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The feeding amount of isobutyraldehyde was controlled to 2.0t/h, and the feeding amount of air was controlled to 150Nm 3 And/h, controlling the flow rate of the liquid phase material in the tube array to be 1.1m/s, controlling the reaction pressure to be 0.2MPaG, and controlling the outlet pressure of the air compressor to be 0.3MPaG, wherein the internal and external pressure difference of the micrometer level distribution tube 77 is about 0.1MPaG, and the reaction product flows out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of the raw isobutyraldehyde was about 95.0%, and the product yield was about 93.6%.
Example 5
(1) The isobutyraldehyde is sent to a liquid phase feed inlet at the bottom of a reactor lower seal head 8 through an external pump, air is sent to a gas phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The feeding amount of isobutyraldehyde was controlled to 2.0t/h, and the feeding amount of air was controlled to 150Nm 3 And/h, controlling the flow rate of the liquid phase material in the tube array to be 1.1m/s, controlling the reaction pressure to be 0.2MPaG, and controlling the outlet pressure of the air compressor to be 0.4MPaG, wherein the internal and external pressure difference of the micrometer level distribution tube 77 is about 0.2MPaG, and the reaction product flows out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of the raw isobutyraldehyde was about 95.6%, and the product yield was about 94.7%.
Example 6
(1) The isobutyraldehyde is sent to a liquid phase feed inlet at the bottom of a reactor lower seal head 8 through an external pump, air is sent to a gas phase feed inlet of a homogeneous distribution section 6 through an external compressor, and a solid catalyst is filled in a reaction column tube 3.
(2) The feeding amount of isobutyraldehyde was controlled to 2.0t/h, and the feeding amount of air was controlled to 150Nm 3 And/h, controlling the flow rate of the liquid phase material in the tube array to be 1.1m/s, controlling the reaction pressure to be 0.2MPaG, and controlling the outlet pressure of the air compressor to be 0.6MPaG, wherein the internal and external pressure difference of the micrometer level distribution tube 77 is about 0.4MPaG, and the reaction product flows out from a discharge port at the top of the upper sealing head 1.
(3) The reaction product was analyzed and assayed, the conversion of raw isobutyraldehyde was about 96.3%, and the product yield was about 95.5%.
Claims (8)
1. A tubular gas-liquid homogeneous reactor is characterized in that: the reactor comprises an upper sealing head, a reaction section, a homogeneous distribution section and a lower sealing head, wherein a discharge hole is formed in the upper end of the upper sealing head, a liquid phase feed inlet is formed in the lower end of the lower sealing head, an upper tube plate is fixedly connected to the upper end of the reaction section, a middle tube plate is fixedly connected between the reaction section and the homogeneous distribution section, a lower tube plate is fixedly connected to the lower end of the homogeneous distribution section, a plurality of reaction tubes are arranged between the upper tube plate and the middle tube plate, a plurality of micron-sized distribution tubes are arranged between the middle tube plate and the lower tube plate, the micron-sized distribution tubes are communicated with the reaction tubes in a one-to-one correspondence manner, and a gas phase feed inlet is formed in the side wall of the homogeneous distribution section between the middle tube plate and the lower tube plate.
2. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the outer diameter of the reaction tube array is 10-150 mm, the wall thickness is 1-8 mm, the length is 500-20000 mm, and the number is 6-10000.
3. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: a spring support is arranged in the reaction tube array; preferably, the height of the spring support is 50-500 mm.
4. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the outer diameter of the micrometer-sized fraction pipe is 10-150 mm, the wall thickness is 1-8 mm, the length is 100-5000 mm, the aperture is 5-1000 mu m, and the number is 6-10000.
5. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the side wall of the lower end of the reaction section between the upper tube plate and the middle tube plate is provided with a heat exchange medium inlet, and the upper end of the reaction section is provided with a heat exchange medium outlet.
6. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the reaction tube also comprises a thermometer, wherein the thermometer is fixedly connected with the upper end socket, and the lower end of the thermometer penetrates through the upper end socket and stretches into the reaction tube array.
7. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the working pressure of the tubular gas-liquid homogeneous reactor is-0.1 to 20MPaG, and the working temperature is-20 to 600 ℃.
8. The shell and tube gas-liquid homogeneous reactor according to claim 1, wherein: the micrometer-scale distribution pipe is one of a metal sintering pipe, a metal wire mesh sintering pipe, a polytetrafluoroethylene microporous pipe and a ceramic microporous pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN202211729791.2A CN116037006A (en) | 2022-12-30 | 2022-12-30 | Tube array type gas-liquid homogeneous reactor |
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| CN202211729791.2A CN116037006A (en) | 2022-12-30 | 2022-12-30 | Tube array type gas-liquid homogeneous reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110420614A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of multiphase flow process intensification reactor |
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2022
- 2022-12-30 CN CN202211729791.2A patent/CN116037006A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110420614A (en) * | 2019-09-02 | 2019-11-08 | 南京中汇能源科技研发中心 | A kind of multiphase flow process intensification reactor |
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