CN223615882U - Propylene carbonylation reaction device - Google Patents
Propylene carbonylation reaction deviceInfo
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- CN223615882U CN223615882U CN202423093739.XU CN202423093739U CN223615882U CN 223615882 U CN223615882 U CN 223615882U CN 202423093739 U CN202423093739 U CN 202423093739U CN 223615882 U CN223615882 U CN 223615882U
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- feed inlet
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- carbonylation reaction
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Abstract
The utility model provides a propylene carbonylation reaction device, which is characterized in that a first reactor of the device is provided with a lower feed inlet for inputting hydrogen and synthesis gas, an upper feed inlet for inputting propylene and catalyst solution, a liquid outlet of the first reactor is connected with the upper feed inlet of the first reactor through a first condenser, a second reactor comprises a shell and a second mixer arranged in the shell, the second reactor is provided with a lower feed inlet for inputting hydrogen and synthesis gas, the liquid outlet of the second reactor is connected with the upper feed inlet of the second reactor through a second condenser, a first branch connected with the upper feed inlet of the second reactor is arranged on a pipeline connected with the liquid outlet of the first reactor and the first condenser, and a gas outlet of the first reactor is connected with the lower feed inlet of the second reactor. The reactor can be independently subjected to temperature regulation and control, so that the temperature fluctuation of the reactor is reduced, and stable production is facilitated.
Description
Technical Field
The utility model relates to the technical field of chemical synthesis, in particular to a propylene carbonylation reaction device.
Background
The butanol-octanol product is an important raw material for basic organic synthesis, and is mainly used for producing plasticizers, solvents, dehydrating agents, defoamers, dispersants, flotation agents, petroleum additives, synthetic fragrances and the like. The wide use of butanol octanol promotes the annual increase in the quantity and yield of butanol octanol.
The process for producing butyraldehyde by propylene low-pressure oxo-synthesis method is most widely applied in the production of butanol and octanol, and the process uses the product n-butyraldehyde as a solvent, propylene, synthesis gas and hydrogen are used for generating n-butyraldehyde and isobutyraldehyde under the action of a catalyst, n-butyl alcohol and isobutanol can be generated by hydrogenating n-butyraldehyde and isobutyraldehyde, n-butyl alcohol and isobutanol products can be obtained by rectifying and separating n-butyraldehyde and isobutyraldehyde by an isomer tower, isobutyraldehyde is used as a byproduct, n-butyraldehyde is condensed and dehydrated under the catalysis of sodium hydroxide to generate octenal, crude octanol is produced by hydrogenating octenal, and the product octanol is obtained by rectifying.
The process flow of the existing propylene carbonylation reaction is shown in figure 1. The core of the process is two oxo reactors, and the specific reaction process comprises the following steps:
The synthesis gas enters the first oxo reactor R-101 from below the impeller at the bottom of the stirrer, the propylene feed, the reaction recycle and the catalyst solution returned by the recycle pump P-101A/B are fed into the first reactor R-101 at a location between the two sets of impellers of the stirrer, and the upper stirring impeller produces an axial flow to thoroughly mix the solution in the reactor while minimizing the temperature gradient of the solution in the reactor. Since the oxo reaction is exothermic, the reaction solution is pumped from the bottom of the reactor by the first reactor circulation pump P-101A/B and cooled by the cooler E-101 of the first reactor, and one part is returned to the first reactor and the other part is returned to the first oxo reactor after passing through the coil inside the second oxo reactor R-102. The reaction liquid containing dissolved catalyst, byproducts and unreacted propylene from R-101 enters a second oxo reactor, synthesis gas is mixed with reaction tail gas from R-101, then enters the bottom of R-102 from the impeller bottom of an agitator A-102 of the R-102 through a gas distributor, purge gas discharged to a reactor emptying condenser E-102 is discharged to a fuel gas main pipe through a demister after condensation, and butyraldehyde and the like condensed in the reactor emptying condenser are returned into the R-102 under the action of gravity.
In the actual process, as the two reactors cooperatively control the temperature and the equipment structure is complex, the cyclic heat load of the first oxo reactor is large, so that the problems of large reactor temperature fluctuation, difficult temperature adjustment of the two reactors, high device maintenance difficulty and the like easily occur in the propylene oxo reaction process.
Disclosure of utility model
Aiming at the defects in the prior art, the utility model discloses a propylene carbonylation reaction device which can be used for independently regulating and controlling the temperature of each reactor, reducing the temperature fluctuation of the reactors and stabilizing the production.
In order to achieve the above technical object, the present utility model provides a propylene carbonylation reaction apparatus comprising:
The device comprises a first reactor, a second reactor, a third reactor, a fourth reactor, a fifth condenser and a third condenser, wherein the first reactor is provided with a lower feed inlet for inputting hydrogen and synthesis gas, an upper feed inlet for inputting propylene and catalyst solution, and a liquid outlet of the first reactor is connected with the upper feed inlet of the first reactor through the first condenser;
The device comprises a first reactor, a second reactor, a first condenser and a second condenser, wherein the first reactor comprises a shell and a first mixer arranged in the shell;
The device comprises a first reactor, a second reactor, a first condenser, a second condenser, a first branch and a second branch, wherein the first branch is arranged on a pipeline connecting a liquid outlet of the first reactor with the first condenser and connected with an upper feed inlet of the second reactor, an air outlet of the first reactor is connected with a lower feed inlet of the second reactor, and the second branch is arranged on a pipeline connecting the liquid outlet of the second reactor with the second condenser and used for outputting reacted materials.
In the utility model, the first reactor and the second reactor are respectively provided with an independent external circulation heat transfer system, wherein the materials reacted in the first reactor are output from a liquid outlet and returned to a feed inlet at the upper part of the reactor after being cooled by a first condenser, so that the aim of regulating and controlling the reaction temperature in the first reactor is fulfilled; compared with the technical characteristics that part of reaction materials of a first reactor are input into a coil pipe in a second reactor to cooperatively control the temperature in the prior art, the utility model reduces the heat load of the first reactor, has higher temperature regulation and control efficiency of the second reactor, ensures that the temperature control of the whole process is more stable, and removes the inner coil pipe in the second reactor, which is difficult to maintain, thereby also reducing the process maintenance difficulty. The second reactor adopts static mixing to replace a stirrer, so that material mixing is promoted, reaction efficiency is improved, and the problem of stirring, sealing and leakage is avoided.
The technical process for carrying out propylene carbonylation reaction by adopting the utility model comprises the following steps:
The method comprises the steps that reaction raw material synthesis gas and hydrogen are input from a lower feed inlet of a first reactor and are mixed with circulating materials which are input from an upper feed inlet and are subjected to heat transfer through a first condenser, meanwhile, raw material propylene and catalyst solution are also input from the upper feed inlet into the first reactor, and most of carbonylation reactions are carried out in the first reactor to generate n-butyraldehyde and isobutyraldehyde;
The reacted material from the first reaction (including catalyst solution, product, by-product and unreacted propylene) is fed into the upper feed inlet of the second reactor, the synthesis gas, hydrogen and unreacted gas phase material from the first reactor are fed into the lower feed inlet of the second reactor, the material fed into the second reactor is fully mixed under the action of the second mixer, and the carbonylation reaction is continuously carried out in the second reactor, and in the reaction process, part of material is fed out from the liquid outlet of the second reactor, condensed by the second condenser and returned to the second reactor, so that the temperature in the reaction is regulated and controlled, and the conversion rate is improved.
Compared with the prior art, the propylene carbonylation reaction device has the beneficial effects that the second reactor is provided with the independent external circulation heat transfer system, so that the second reactor is independently subjected to temperature regulation and control, the circulation heat load of the first reactor is reduced, the temperature control stability of the whole process is facilitated, a mixer is arranged in the second reaction to replace a traditional mixer, the reaction materials are promoted to be fully mixed, the reaction conversion rate is improved, meanwhile, the stirring sealing leakage problem is avoided while the process equipment is simplified, and the equipment investment and maintenance cost is reduced.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model. In the drawings:
FIG. 1 shows a prior art propylene carbonylation structure;
The drawing comprises the following reference numerals of a first oxo reactor of R-101, a cooler of a first oxo reactor of E-101, a P-101A/B circulating pump, a second oxo reactor of R-102 and a venting condenser of the E-102.
FIG. 2 shows a structural view of the propylene carbonylation reaction apparatus of the present utility model.
Wherein the above figures include the following reference numerals:
1-first reactor, 11-first mixer, 2-second reactor, 21-second mixer, 31-first condenser, 32-second condenser, 33-third condenser, 41-first branch, 42-second branch, 43-third branch, 44-fourth branch, 45-fifth branch, 5-gas distributor, 6-condensate tank, 71-liquid level gauge, 72-first switch valve, 73-second switch valve, 74-thermometer.
Detailed Description
In order that the utility model may be understood more fully, a more particular description of the utility model will be rendered by reference to preferred embodiments thereof. It should be understood that these examples are for the purpose of more detailed description only and should not be construed as limiting the utility model in any way, i.e., not intended to limit the scope of the utility model.
Unless defined otherwise, technical terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which the inventive concepts pertain. The test reagents used in the following examples are all conventional biochemical reagents unless otherwise specified, and the test methods are all conventional methods unless otherwise specified.
Example 1
A propylene carbonylation reaction apparatus, as shown in figure 1, comprising:
The first reactor 1 is provided with a lower feed inlet for inputting hydrogen and synthesis gas, an upper feed inlet for inputting propylene and catalyst solution, and a liquid outlet of the first reactor 1 is connected with the upper feed inlet of the first reactor 1 through a first condenser 31;
The second reactor 2 comprises a shell and a second mixer 21 arranged in the shell, wherein the second reactor 2 is provided with a lower feed inlet for inputting hydrogen and synthesis gas, and a liquid outlet of the second reactor 2 is connected with an upper feed inlet of the second reactor 2 through a second condenser 32;
The pipeline connecting the liquid outlet of the first reactor 1 and the first condenser 31 is provided with a first branch 41 connected with the upper feed inlet of the second reactor 2, the gas outlet of the first reactor 1 is connected with the lower feed inlet of the second reactor 2, and the pipeline connecting the liquid outlet of the second reactor 2 and the second condenser 32 is provided with a second branch 42 for outputting the reacted materials.
Compared with the prior art, (1) the technical scheme removes the inner coil in the second reactor 2, adds an external circulation reaction heat transfer system comprising the second condenser 32, realizes the effects of strengthening the cooling of the reaction materials of the second reactor 2 and reducing the temperature fluctuation of the first reactor 1, thereby stabilizing the production, and in addition, the traditional inner coil heat transfer maintenance is very difficult, and the effective operation time can be increased after the traditional inner coil heat transfer maintenance is removed. (2) According to the technical scheme, the mixer is adopted to replace a stirrer in the prior art, the problem of stirring, sealing and leakage is avoided, meanwhile, the mixer is additionally arranged in the shell, so that the reaction materials can be more fully mixed, and the reaction conversion rate is improved.
It should be noted that the present utility model is not limited to the source of the catalyst solution fed into the first reactor 1, and the catalyst solution may be selected from a downstream product-catalyst separation process, a catalyst washing process, a catalyst disposition process, etc., or a mixed catalyst solution in which a plurality of sources of catalyst solutions are dissolved.
It should be noted that the source of the material fed into the lower inlet of the second reactor 2 is not limited in the present utility model, and the use of the lower inlet does not limit the scope of the present utility model. If only propylene and synthesis gas are used as raw materials in the specific carbonylation reaction, the lower feed inlet of the first reaction summation second reactor 2 is used for inputting synthesis gas, and if synthesis gas and hydrogen are used as raw materials in the specific carbonylation reaction, the lower feed inlet of the first reaction summation second reactor 2 is used for inputting synthesis gas and hydrogen, or in specific working conditions, the synthesis gas and hydrogen from new input, unreacted materials from the first reactor 1, separated gas from a subsequent product-catalyst separation procedure, and the like, or mixed materials of the materials from the above sources are not used for limiting the protection scope of the utility model.
Optionally, the lower feed inlet of the second reactor 2 comprises two secondary feed inlets arranged up and down, so that layering control is conveniently performed in the actual process according to the difference of gas phase material compositions input into the lower feed inlet of the second reactor 2, and the reaction efficiency in the second reactor 2 is improved.
It should be noted that the specific structure of the second mixer is not limited by the present utility model, and those skilled in the art may select a component or a device capable of promoting mixing of materials based on the present utility model, and the optional second mixer includes a plurality of layers of porous distribution plates arranged up and down, the gas phase materials for inputting reaction are input through a connecting pipeline at the bottom of the porous distribution plates, the circulating liquid is input through a connecting pipeline at the upper part of the porous distribution plates, and the reacted materials laterally flow out of the mixer through reverse contact reaction, so that static mixing of the materials in the input reactor is realized.
Example 2
The structure of the first reactor 1 was optimized based on the propylene carbonylation reaction apparatus shown in example 1.
Optionally, the first reactor 1 includes a housing and a first mixer 11 disposed in the housing, and the first mixer 11 is used to replace a stirrer disposed in the first reactor 1 in the prior art, so that the problem of sealing leakage of the stirrer in the first reactor 1 can be avoided, and the safety of the device is further improved.
It is noted that the utility model is not limited to the specific configuration of the first mixer and one skilled in the art can select components or devices to promote mixing of materials based on the utility model to promote static mixing of materials fed into the reactor.
Example 3
Based on the propylene carbonylation reaction apparatus shown in example 1 or example 2, the lower feed inlet of the first reactor 1 and/or the second reactor 2 in this example is connected to the gas distributor 5, so as to promote the gas phase raw material fed from the lower feed inlet to be fully mixed with the materials in the reactor, and improve the reaction efficiency.
Example 4
Based on the propylene carbonylation reaction apparatus shown in example 1, the structure of the second reactor 2 to which the gas outlet is connected was optimized in this example.
Optionally, the gas phase outlet of the second reactor 2 is connected to the condensate tank 6 through the third condenser 33, so that the product separated from the gas outlet is condensed by the third condenser 33 and then subjected to gas-liquid separation, the condensed condensate obtained by condensation is collected in the condensate tank 6 and is output from the liquid outlet of the condensate tank 6, and then enters the downstream product-catalyst separation process, thereby avoiding the accumulation of propane carried by butyraldehyde condensate after directly returning to the reactor and improving the product yield.
Further alternatively, the condensate tank 6 is provided with a liquid level gauge 71, a pipeline connected with a liquid outlet of the condensate tank 6 is provided with a first switch valve 72 in signal communication with the liquid level gauge 71, and the discharge of condensate is regulated and controlled through the interlocking of the liquid level gauge 71 and the first switch valve 72, so that the process automation level is improved.
Further alternatively, the gas phase outlet of the third condenser 33 and/or the gas phase outlet of the condensate tank 6 are connected to a fuel gas pipe network, and purge gas discharged from the third condenser 33 and the condensate tank 6 may be input to a subsequent fuel gas pipe network for treatment.
Example 5
The present embodiment optimizes the connection structure of the second condenser 32 based on the propylene carbonylation reaction apparatus shown in embodiment 1.
Optionally, a third branch 43 connected to the rear end of the second condenser 32 is provided at the front end of the second condenser 32, and a second switch valve 73 is provided on the third branch 43, so that the proportion of the external circulation material of the second reactor 2 condensed by the second condenser 32 can be adjusted according to the working condition requirement in the actual operation process, and the material output from the liquid outlet of the second reactor 2 can be partially returned to the second reactor 2 without being condensed by the second condenser 32 under some special working conditions, thereby reducing the process energy consumption and improving the operability of temperature adjustment.
Further alternatively, a thermometer 74 in signal communication with the second switch valve 73 is provided on a pipeline connected to the second condenser 32, so that the utility model can automatically adjust the proportion of the circulating material condensed by the second condenser 32 according to the temperature of the external circulating material in specific working conditions.
Example 6
Based on the propylene carbonylation reaction apparatus shown in embodiment 1, in this embodiment, the rear end of the first condenser 31 is provided with a fourth branch 44 connected to the front end thereof, and the fourth branch 44 is configured to partially mix the material condensed by the first condenser 31 with the material reacted in the first reactor 1 under certain working conditions, so as to facilitate controlling the temperature in the first reactor 1.
In some optional examples of the present utility model, an interlocking thermometer and a switch valve may be optionally disposed on the fourth branch 44, so as to adjust the flow rate of the circulating material passing through the fourth branch 44 according to the temperature of the circulating material condensed by the first condenser 31 and the temperature in the first reactor 1, thereby improving the convenience of process temperature adjustment.
Example 7
Based on the propylene carbonylation reaction apparatus shown in embodiment 1, the rear end of the second condenser 32 in this embodiment is provided with a fifth branch 45 connected to the front end thereof, and the fifth branch 45 is used for partially mixing the material condensed by the second condenser 32 with the material reacted by the second reactor 2 under certain working conditions, so as to be beneficial to regulating and controlling the temperature in the second reactor 2.
In some optional examples of the present utility model, an interlocking thermometer and a switch valve may be optionally disposed on the fifth branch 45, so as to adjust the flow rate of the circulating material passing through the fifth branch 45 according to the temperature of the circulating material condensed by the first condenser 31 and the temperature in the second reactor 2, thereby improving the convenience of process temperature adjustment.
It should be noted that, to promote the improvement of the process efficiency, those skilled in the art may use the present utility model to provide a device or apparatus for improving the material circulation efficiency, such as a circulation pump, a compressor, etc. on a pipeline for circulating the liquid phase material or the gas phase material, and the present utility model is not limited to the scope of protection thereof.
It should be noted that, based on the present utility model, those skilled in the art may optionally provide an on-off valve and a thermometer, a flowmeter, a manometer, or a level meter, a thermometer, a manometer, etc. disposed on the reactor and interlocked with the on-off valve on the material flow pipeline, so as to facilitate the automatic operation of the present utility model, but not limit the protection scope of the present utility model.
It should be noted that the above description is further detailed description of the present utility model in connection with the specific embodiments, and the implementation of the present utility model should not be construed as limited to the descriptions, but the dimensional data of the present embodiment should not be construed as limiting the technical solution, but merely as showing one of the specific working conditions. It will be apparent to those skilled in the art that several simple modifications and adaptations of the utility model can be made without departing from the spirit of the utility model and are intended to be within the scope of the utility model.
Claims (10)
1. A propylene carbonylation reaction apparatus comprising:
The device comprises a first reactor (1), wherein the first reactor (1) is provided with a lower feed inlet for inputting hydrogen and synthesis gas, an upper feed inlet for inputting propylene and catalyst solution, and a liquid outlet of the first reactor (1) is connected with the upper feed inlet of the first reactor (1) through a first condenser (31);
The device comprises a first reactor (2), wherein the first reactor (2) comprises a shell and a first mixer (21) arranged in the shell, the first reactor (2) is provided with a first condenser (32) and a second condenser (32), the first condenser is connected with the first mixer, and the second condenser is connected with the second mixer;
The device comprises a first reactor (1), a second reactor (2), a first condenser (31), a second condenser (32) and a first branch (41) connected with the upper feed inlet of the second reactor, wherein the first branch (41) is arranged on a pipeline connecting the liquid outlet of the first reactor (1) and the first condenser, the gas outlet of the first reactor (1) is connected with the lower feed inlet of the second reactor (2), and the second branch (42) for outputting reacted materials is arranged on a pipeline connecting the liquid outlet of the second reactor (2) and the second condenser (32).
2. The propylene carbonylation reaction device according to claim 1, characterized in that the first reactor (1) comprises a housing and a first mixer (11) provided in the housing.
3. Propylene carbonylation reaction device according to claim 1 or 2, characterized in that the lower feed inlet of the first reactor (1) and/or the second reactor (2) is connected to a gas distributor (5).
4. Propylene carbonylation reaction device according to claim 1, characterized in that the gas phase outlet of the second reactor (2) is connected to a condensate tank (6) via a third condenser (33).
5. The propylene carbonylation reaction device according to claim 4, wherein the condensate tank (6) is provided with a liquid level meter (71), and a first switch valve (72) in signal communication with the liquid level meter (71) is arranged on a pipeline connected with a liquid outlet of the condensate tank (6).
6. Propylene carbonylation reaction device according to claim 4 or 5, characterized in that the gas phase outlet of the third condenser (33) and/or the gas phase outlet of the condensate tank (6) is connected to a fuel gas pipe network.
7. The propylene carbonylation reaction device according to claim 1, wherein a third branch (43) connected to the rear end of the second condenser (32) is provided at the front end of the second condenser, and a second switch valve (73) is provided on the third branch (43).
8. The propylene carbonylation reaction apparatus according to claim 7, wherein a thermometer (74) in signal communication with the second on-off valve (73) is provided on a line connected to the second condenser (32).
9. Propylene carbonylation reaction device according to claim 1, characterized in that the rear end of the first condenser (31) is provided with a fourth branch (44) connected to its front end, said fourth branch (44) being adapted to partly mix the material condensed by the first condenser (31) with the material reacted by the first reactor (1).
10. Propylene carbonylation reaction device according to claim 1, characterized in that the rear end of the second condenser (32) is provided with a fifth branch (45) connected to the front end thereof, said fifth branch (45) being adapted to partly mix the material condensed by the second condenser (32) with the material reacted by the second reactor (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202423093739.XU CN223615882U (en) | 2024-12-16 | 2024-12-16 | Propylene carbonylation reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202423093739.XU CN223615882U (en) | 2024-12-16 | 2024-12-16 | Propylene carbonylation reaction device |
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| Publication Number | Publication Date |
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| CN223615882U true CN223615882U (en) | 2025-12-02 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
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| CN202423093739.XU Active CN223615882U (en) | 2024-12-16 | 2024-12-16 | Propylene carbonylation reaction device |
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| CN (1) | CN223615882U (en) |
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