CN216024778U - Reaction system for hydroformylation reaction - Google Patents
Reaction system for hydroformylation reaction Download PDFInfo
- Publication number
- CN216024778U CN216024778U CN202121922766.7U CN202121922766U CN216024778U CN 216024778 U CN216024778 U CN 216024778U CN 202121922766 U CN202121922766 U CN 202121922766U CN 216024778 U CN216024778 U CN 216024778U
- Authority
- CN
- China
- Prior art keywords
- gas
- reaction
- channel
- communicated
- reaction system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides a reaction system for hydroformylation reaction, which at least comprises a reaction kettle, wherein the reaction kettle comprises a kettle body, a Venturi ejector and a gas distribution plate; the gas distribution plate is arranged in the kettle body and divides the kettle body into a gas-liquid contact reaction cavity and a gas material chamber; the venturi ejector is positioned at the top of the kettle body, and a material outlet of the venturi ejector is positioned in the gas-liquid contact reaction cavity; the bottom of the gas-liquid contact reaction cavity is connected with a reaction material outlet channel; the gas material chamber is communicated with a gas material inlet channel. Reaction system is used for the area of contact and the continuous renewal that the hydroformylation reaction can increase the gas-liquid in this application, has strengthened the mass transfer effect, and it can improve reaction conversion, shortens reaction time greatly to the reaction can go on in succession.
Description
Technical Field
The utility model relates to the field of chemical reaction preparation, in particular to a reaction system for hydroformylation.
Background
The hydroformylation of olefins refers to a process in which carbon monoxide and hydrogen are reacted with olefins in the presence of a catalyst under pressure to form aliphatic aldehydes having one more carbon atom than the olefins used, and is also called "hydroformylation".
Aqueous catalyst solution, CO/H, in hydroformylation of olefins2And the product aldehyde forms a gas-liquid three phase, so that a slurry bed reactor is adopted for the reaction.
Chinese patent CN 111217686A introduces a Venturi ejector type reactor, which has the advantages that the static pressure energy and the kinetic energy are skillfully used for realizing the circulation of reaction gas, and the energy consumption is reduced; the disadvantage is that the molar ratio of recycle gas to fresh gas which is involved in the reaction is not high.
A shell-and-tube hydroformylation reactor is introduced in Chinese patent CN 208554115U, the reactor breaks through the limitation of the traditional reactor on gas-liquid two-phase mass transfer and heat transfer rate, improves the heat transfer and mass transfer efficiency, but for high-carbon aldehyde, the high-carbon aldehyde is easy to crystallize and separate out at a position close to the tube wall to block the tube.
A bottom-spraying self-suction reactor is introduced in a Chinese patent CN 210560168U, the principle is the same as that of a patent CN 111217686A, on the basis, a bottom gas distribution pipe is additionally arranged, fresh supplementary hydrogen and a recycle hydrogen part are sucked into an ejector at the top end, and a part of the fresh supplementary hydrogen and the recycle hydrogen part enter a gas distributor at the bottom of a kettle, so that the defect of limited recycle gas amount is overcome to a certain extent, but the annular distributor still has the condition of uneven gas distribution.
SUMMERY OF THE UTILITY MODEL
In view of the above-mentioned shortcomings of the prior art, the present invention is directed to a reaction system for hydroformylation, which has the characteristics of high heat and mass transfer efficiency, and is used to solve the above-mentioned problems of the prior art reactors for hydroformylation, such as limited gas circulation of venturi injector, uneven gas distribution of annular gas distribution plate, etc., which have the disadvantages of low heat and mass transfer efficiency and prolonged reaction time of the hydroformylation reactor.
To achieve the above objects and other related objects, the present invention includes the following technical solutions.
The utility model provides a reaction system for hydroformylation reaction, which comprises a reaction kettle, wherein the reaction kettle comprises a kettle body, a Venturi ejector and a gas distribution plate; the gas distribution plate is arranged in the kettle body and divides the kettle body into a gas-liquid contact reaction cavity and a gas material chamber; the venturi ejector is positioned at the top of the kettle body, and a material outlet of the venturi ejector is positioned in the gas-liquid contact reaction cavity; the bottom of the gas-liquid contact reaction cavity is connected with a reaction material outlet channel; the gas material chamber is connected with a gas material inlet channel.
Preferably, the venturi ejector comprises an inlet section, a nozzle, a mixing section and a diffuser section which are communicated in sequence; and air chambers are arranged around the periphery of the inlet section and the nozzle and communicated with the mixing section.
Preferably, the reaction system further comprises a reaction liquid feed passage, which is in communication with the material inlet of the venturi ejector. More preferably, the reactant liquid feed passage communicates with the inlet section of the venturi ejector.
Preferably, the reaction system further comprises a reaction liquid circulation channel, one end of the reaction liquid circulation channel is communicated with the liquid material outlet channel, and the other end of the reaction liquid circulation channel is communicated with the material inlet of the venturi ejector. More preferably, the other end of the reaction liquid circulation assembly communicates with the inlet section of the venturi ejector.
More preferably, a circulating pump and/or a condenser are/is further arranged on the reaction liquid circulating channel.
More preferably, a storage channel is further connected to the reaction liquid circulation channel. The storage channel is used for storing part of reaction liquid in the circulation process for later use.
Preferably, the reactor further comprises a central gas channel, the central gas channel is connected with the gas distribution plate, and the gas material inlet channel is communicated with the gas-liquid contact reaction cavity through the central gas channel.
Preferably, a compressor is further arranged on the gas material inlet channel communicated with the gas material chamber.
Preferably, a compressor is further arranged on the gas material inlet channel communicated with the gas-liquid contact reaction cavity.
Preferably, the top of the gas-liquid contact reaction cavity is also communicated with a circulating gas outlet channel, and the circulating gas outlet channel is communicated with the gas material inlet channel provided with a compressor.
Preferably, the central gas channel is divided into a plurality of branch channels at one end, and the ends of the plurality of branch channels are connected to the gas distribution plate.
More preferably, the branch channels are connected to the same height of the gas distribution plate, and the included angle between two adjacent branch channels is the same.
Preferably, the gas distribution plate is of a tapered structure along a top-down direction. More preferably, the gas distribution plate has a conical or truncated cone shape in profile. More preferably, the gas distribution plate is at an angle of no more than 45 ° to the horizontal.
As described above, the reaction system of the present invention has the following advantageous effects:
reaction system is used for the area of contact and the continuous renewal that the hydroformylation reaction can increase the gas-liquid in this application, has strengthened the mass transfer effect, and it can improve reaction conversion, shortens reaction time greatly to the reaction can go on in succession.
Drawings
FIG. 1 is a schematic view showing the structure of a reaction system for hydroformylation according to the present invention.
The reference numerals in fig. 1 are explained as follows: 1 is a kettle body, 2 is a Venturi ejector, 3 is a gas distribution plate, 11 is a gas-liquid contact reaction cavity, 12 is a gas material chamber, 4 is a reaction material outlet channel, 5 is a gas material inlet channel, 51 is a circulating gas outlet channel, 52 a first gas inlet section, 53 a second gas inlet section, 6 is a reaction liquid feeding channel, 7 is a reaction liquid circulating channel, 71 is a circulating pump, 72 is a condenser, 73 is a material storage channel, 8 is a central gas channel, 9 is a compressor, and 10 is a circulating gas outlet channel.
Detailed Description
The following description of the embodiments of the present invention is provided for illustrative purposes, and other advantages and effects of the present invention will become apparent to those skilled in the art from the present disclosure.
Please refer to fig. 1. It should be understood that the structures, ratios, sizes, and the like shown in the drawings and described in the specification are only used for matching with the disclosure of the specification, so as to be understood and read by those skilled in the art, and are not used to limit the conditions under which the present invention can be implemented, so that the present invention has no technical significance, and any structural modification, ratio relationship change, or size adjustment should still fall within the scope of the present invention without affecting the efficacy and the achievable purpose of the present invention. In addition, the terms "upper", "lower", "left", "right", "middle" and "one" used in the present specification are for clarity of description, and are not intended to limit the scope of the present invention, and the relative relationship between the terms and the terms is not to be construed as a scope of the present invention.
As shown in fig. 1, a specific reaction system for hydroformylation is provided, the reaction system at least comprises a reaction kettle, the reaction kettle comprises a kettle body 1, a venturi ejector 2 and a gas distribution plate 3; the gas distribution plate 3 is arranged in the kettle body 1 and divides the kettle body 1 into a gas-liquid contact reaction cavity 11 and a gas material chamber 12; the venturi ejector 2 is positioned at the top of the kettle body 1, and a material outlet of the venturi ejector 2 is positioned in the gas-liquid contact reaction cavity 11; the bottom of the gas-liquid contact reaction cavity 11 is connected with a reaction material outlet channel 4; the gas material chamber 12 is connected with a gas material inlet channel 5. In fig. 1, the first gas inlet section 52 in fig. 1 communicates with the gas material chamber 12, so that gas enters the gas material chamber.
In a preferred embodiment, the venturi ejector 2 comprises an inlet section, a nozzle, a mixing section and a diffuser section in series; and air chambers are arranged around the periphery of the inlet section and the nozzle and communicated with the mixing section.
In a preferred embodiment, the reaction system further comprises a reaction liquid feed channel 6, the reaction liquid feed channel 6 being in communication with the feed inlet of the venturi ejector 2. More preferably, the reaction liquid feed channel 6 communicates with the inlet section of the venturi ejector 2.
In a preferred embodiment, the reaction system further comprises a reaction liquid circulation channel 7, one end of the reaction liquid circulation channel 7 is communicated with the reaction material outlet channel 4, and the other end is communicated with the material inlet of the venturi ejector 2. More preferably, the other end of the reaction liquid circulation passage 7 communicates with the inlet section of the venturi ejector 2.
In a preferred embodiment, the reaction liquid circulation channel 7 is further provided with a circulation pump 71 and/or a condenser 72.
In a preferred embodiment, the reaction liquid circulation channel 7 is also communicated with a storage channel 73. The storage channel 73 is used for storing part of the reaction liquid in the circulation process for later use.
In a preferred embodiment, the gas outlet end of the gaseous feed inlet channel 5 is also in communication with the venturi ejector 2.
In a preferred embodiment, the reaction system further comprises a central gas channel 8, the central gas channel 8 is connected with the gas distribution plate 3, and the gas material inlet channel 5 is further communicated with the gas-liquid contact reaction chamber 11 through the central gas channel 8. The second gas inlet section 53, as shown in fig. 1 in particular, communicates with the gas-liquid contact reaction chamber 11 through the central gas passage 8.
In a preferred embodiment, a compressor 10 is also provided in the gas feed inlet channel communicating with the gas feed chamber 12.
In a preferred embodiment, a compressor 10 is further provided on the gas material inlet passage communicating with the gas-liquid contact reaction chamber 11.
In a preferred embodiment, the top of the gas-liquid contact reaction chamber 11 is also communicated with a circulating gas outlet channel 51, and the circulating gas outlet channel 51 is communicated with the gas material inlet channel 5 provided with a compressor.
In a preferred embodiment, the central gas channel 8 is divided at one end into a plurality of branch channels, the ends of which are connected to the gas distribution plate 3.
More preferably, the branch channels are connected to the same height of the gas distribution plate 3, and the included angle between two adjacent branch channels is the same.
Preferably, the gas distribution plate 3 has a tapered structure along a top-down direction. More preferably, the profile of the gas distribution plate 3 is conical or truncated cone-shaped. More preferably, the gas distribution plate 3 is at an angle of no more than 45 ° to the horizontal.
When the reaction device is used, reaction liquid is added into the gas-liquid contact reaction cavity 11 through the reaction liquid feeding channel 6, the reaction liquid in the gas-liquid contact reaction cavity 11 enters the reaction liquid circulating channel 7 through the reaction material outlet channel 4, the pressure is increased through the circulating pump 71 and then the reaction liquid is sprayed through the Venturi ejector 2, the reaction circulating liquid generates extremely high flow speed, pressure drop is formed around the nozzle, part of circulating and fresh feeding mixed gas supplied by the gas chamber is sucked into the gas chamber, and then the mixed gas is fully mixed in the mixing section to form turbulence and continuously react. The flow velocity of the product in the diffusion section begins to be slowly reduced, the product is sent out by utilizing the static pressure converted by the kinetic energy, and a large amount of gas can be automatically sucked by partial gas without the pressure increase of a compressor and other motive equipment, so that the energy consumption is reduced. And the material is sprayed out of the nozzle and then passes through a jet flow area, a mixing oscillation area and a foam area, namely, a gas phase is changed from a continuous phase to a dispersed phase, a liquid phase is still the continuous phase, in the mixing section, the jet flow is suddenly changed into a foam flow, the gas flow is dispersed in the liquid in a bubble shape, at the moment, the gas phase and the liquid phase are in a highly mixed state, the contact surface is greatly increased and continuously updated, the mass transfer is extremely rapid, the gas-liquid phase reaction controlled by diffusion is very favorable, and the reaction time can be greatly reduced.
In the application, through the control of the gas flow in the gas material inlet channel 5, the circulating gas outlet channel 51, the first gas inlet section 52 and the second gas inlet section 53 and the control of the opening size and the opening rate of the holes on the gas distribution plate 3, the gas material in the gas material chamber 12 can enter the gas-liquid contact reaction chamber 11 through the holes in the gas distribution plate 3, and the liquid in the gas-liquid contact reaction chamber 11 cannot leak into the gas material chamber 12.
Combine the circulation channel and the design of reaction gas and reaction liquid in this application for the two-phase intensive mixing of gas-liquid has increased the area of contact of gas-liquid and has constantly updated, can make the reaction go on in succession moreover.
Compared with a slurry bed reaction kettle in the prior art, the reaction time is greatly shortened, preferably less than 2 hours, on the premise of keeping the same conversion rate and the same direct-to-differential ratio to be more than or equal to 17.
The following is a reaction system using the hydroformylation reaction shown in fig. 1, and the specific structure and parameters thereof are as follows:
structural design of a reaction system: the height of the kettle body 1 is 300mm, and the diameter is 150 mm. The nozzle of the venturi eductor 2 has a diameter of about 7mm, a nozzle-to-mixing section inlet distance of > 50mm and < 100mm, and a mixing section and a diffuser section length of greater than 150 mm. The gas distribution plate 3 is conical, the included angle between the gas distribution plate 3 and the horizontal plane is 45 degrees, the aperture diameter phi of the opening on the gas distribution plate 3 is 4-5 mm, and the aperture ratio is less than 1%.
Conditions for carrying out the reaction: reaction temperature: the reaction pressure is 3.1MPa (A) at 100 ℃; reactor feed inlet conditions: catalyst aqueous solution feed flow rate: 1m3Hour/hour; high olefin feed flow rate: 0.5m3Hour/hour; CO + H2Feeding flow rate: 3Nm3Hour/hour; CO: H2In a 1:1 molar ratio.
Discharging results at the discharging port: high carbene conversion: 95 percent; product selectivity: more than or equal to 80 percent.
In the embodiment, the production process of preparing the high carbon aldehyde by the hydroformylation reaction of the high carbon olefin is realized by the high carbene conversion rate of 95 percent and the product selectivity of more than or equal to 80 percent.
Therefore, the utility model effectively overcomes various defects in the prior art and has high industrial utilization value.
The foregoing embodiments are merely illustrative of the principles and utilities of the present invention and are not intended to limit the utility model. Any person skilled in the art can modify or change the above-mentioned embodiments without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which can be made by those skilled in the art without departing from the spirit and technical spirit of the present invention be covered by the claims of the present invention.
Claims (10)
1. A reaction system for hydroformylation reaction is characterized by at least comprising a reaction kettle, wherein the reaction kettle comprises a kettle body (1), a Venturi ejector (2) and a gas distribution plate (3); the gas distribution plate (3) is arranged in the kettle body (1) and divides the kettle body (1) into a gas-liquid contact reaction cavity (11) and a gas material chamber (12); the Venturi ejector (2) is arranged at the top of the kettle body (1), and a material outlet of the Venturi ejector (2) is positioned in the gas-liquid contact reaction cavity (11); the bottom of the gas-liquid contact reaction cavity (11) is connected with a reaction material outlet channel (4); the gas material chamber (12) is communicated with a gas material inlet channel (5).
2. The reaction system according to claim 1, wherein the venturi ejector (2) comprises an inlet section, a nozzle, a mixing section and a diffuser section, which are in communication in sequence; the periphery of the inlet section and the nozzle is annularly provided with air chambers which are communicated with the mixing section; and/or, along the direction from top to bottom, the gas distribution plate (3) is of a reducing structure.
3. The reaction system according to claim 1, further comprising a reaction liquid feed channel (6), the reaction liquid feed channel (6) communicating with a material inlet of the venturi ejector (2); and/or the reaction system further comprises a reaction liquid circulating channel (7), one end of the reaction liquid circulating channel (7) is communicated with the reaction material outlet channel (4), and the other end of the reaction liquid circulating channel is communicated with the material inlet of the Venturi ejector (2).
4. The reaction system according to claim 3, wherein the reaction liquid circulation channel (7) is further provided with a circulation pump (71) and/or a condenser (72); and/or the reaction liquid circulating channel (7) is also communicated with a storage channel (73).
5. A reaction system according to claim 1, wherein the gas outlet end of the gaseous feed inlet channel (5) is also in communication with the venturi ejector (2).
6. The reaction system according to claim 5, further comprising a central gas channel (8), wherein the central gas channel (8) is connected to the gas distribution plate (3), and the gas material inlet channel (5) is communicated with the gas-liquid contact reaction chamber (11) through the central gas channel (8).
7. A reaction system according to claim 5 or 6, characterized in that a compressor (10) is further provided on the gas material inlet channel communicating with the gas material chamber (12); and/or a compressor (10) is also arranged on a gas material inlet channel communicated with the gas-liquid contact reaction cavity (11).
8. The reaction system according to claim 1, wherein the top of the gas-liquid contact reaction chamber (11) is further communicated with a recycle gas outlet passage (51), and the recycle gas outlet passage (51) is communicated with the gas material inlet passage provided with a compressor.
9. The reaction system according to claim 6, wherein the central gas channel (8) is divided at one end into a plurality of branch channels, and the ends of the plurality of branch channels are connected to the gas distribution plate (3).
10. The reaction system of claim 9, wherein the branched channels are connected to the same height of the gas distribution plate (3), and the included angle between two adjacent branched channels is the same.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121922766.7U CN216024778U (en) | 2021-08-16 | 2021-08-16 | Reaction system for hydroformylation reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121922766.7U CN216024778U (en) | 2021-08-16 | 2021-08-16 | Reaction system for hydroformylation reaction |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN216024778U true CN216024778U (en) | 2022-03-15 |
Family
ID=80620226
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121922766.7U Active CN216024778U (en) | 2021-08-16 | 2021-08-16 | Reaction system for hydroformylation reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN216024778U (en) |
-
2021
- 2021-08-16 CN CN202121922766.7U patent/CN216024778U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP2007530275A (en) | Slurry bubble column reactor | |
| CN107930555B (en) | Multistage horizontal stirring airlift reactor for preparing ethylbenzene hydroperoxide and application | |
| CN216024778U (en) | Reaction system for hydroformylation reaction | |
| CN108479640B (en) | Gas distributor and system containing same | |
| CN106076237B (en) | Tubulation couples microchannel alkylation reactor and its application with fixed bed | |
| CN113750913A (en) | Reaction system for hydroformylation reaction | |
| CN2187492Y (en) | Self-suction high-effect circular flow gas/liquid reactor | |
| CN112479822A (en) | Enhanced micro-interface reaction system and method for preparing ethylene glycol by oxalate method | |
| CN212731735U (en) | Loop reaction ejector | |
| WO2000027514A1 (en) | Ejector for entraining a gas into a liquid | |
| CN213644075U (en) | Microbubble generator and hydrocarbon oil hydrogenation reactor | |
| CN205676168U (en) | A kind of carburizing reagent system of injection reactor and nano-calcium carbonate | |
| CN112791672A (en) | Bubble column reaction combination unit | |
| CN104387258B (en) | A kind of production of chloroacetic acid method and chlorination reactor | |
| CN208824451U (en) | A kind of new and effective methyl alcohol synthetic reactor | |
| CN209020391U (en) | A kind of bubbling column reactor | |
| CN220531526U (en) | Dimethylformamide reactor for preventing bottom crystals from gathering | |
| CN105800659A (en) | Spraying reactor and carbonization reaction system of nano calcium carbonate | |
| CN218077821U (en) | Oxidation equipment for producing trimellitic anhydride | |
| CN105214578A (en) | Gas-liquid reactor and gas-liquid reactor group | |
| CN112427002B (en) | Tower-type superfine contact reaction device for biodiesel | |
| CN215963488U (en) | Reactor | |
| CN205182694U (en) | Gas liquid reaction ware and gas liquid reaction ware group | |
| CN219765352U (en) | membrane reactor | |
| CN111167385B (en) | Jet type gas-liquid reactor for preparing acid by utilizing aldehyde raw material and air |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |