CN217288430U - Tower kettle reactor - Google Patents
Tower kettle reactor Download PDFInfo
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- CN217288430U CN217288430U CN202221207899.0U CN202221207899U CN217288430U CN 217288430 U CN217288430 U CN 217288430U CN 202221207899 U CN202221207899 U CN 202221207899U CN 217288430 U CN217288430 U CN 217288430U
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Abstract
The utility model relates to a tower kettle reactor, which comprises a reactor body, wherein the reactor body comprises a reaction kettle and a reaction tower which is integrally connected with the top end of the reaction kettle, and the reaction kettle is provided with a main feed inlet; the reaction tower is internally provided with a corrugated carrier, a circulating flow guide device is arranged beside the reaction tower, and a liquid reactant enters the reaction kettle from the main feed inlet to reach a preset filling amount and is guided into the reaction tower by the circulating flow guide device to flow back to the reaction kettle from the upper part of the corrugated carrier; and a blowing pipe for blowing the vaporous reactants is arranged in the reaction kettle and is close to the kettle bottom. The utility model discloses an integrated setting of reation kettle and reaction tower makes reaction volume improve greatly to practice thrift the area that occupies, carry out the secondary reaction through circulation guiding device with liquid reactant guide whereabouts and ascending vapour attitude reactant in the reaction tower and also shortened reaction time and improvement reaction efficiency.
Description
Technical Field
The utility model belongs to the technical field of organic synthesis, especially, relate to a tower cauldron reactor.
Background
At present, in the preparation of esters, the esters are generally prepared by reacting acid compounds and alcohol compounds under other conditions such as catalysis and heating, for example, fatty acids and alkyl alcohols are subjected to esterification reaction under the action of a catalyst during heating, and fatty acid esters are generated after dehydration of the products. The palmitic acid and the isopropanol are heated and esterified under the action of sulfuric acid catalysis, and isopropyl palmitate is obtained after dehydration of the product.
The existing fatty acid ester production method is as follows: taking an example of synthesizing isopropyl palmitate, adding palmitic acid, isopropanol and a catalyst into an enamel reaction kettle with a stirrer, heating, keeping the temperature in the kettle at about 90 ℃, and continuously stirring. However, the reaction production carried out under this apparatus has the following disadvantages: 1. the volume is small, the materials which can be added are limited and react in a small container, and the reaction time is longer; 2. the conversion rate of the reaction is low, and if the stirring is insufficient, the quality of the reaction product is also poor.
Disclosure of Invention
In order to solve the technical problem, the utility model provides an at first tower cauldron reactor can react many times when improving reaction volume, need not to consider the problem of installation such as stirring rake, motor simultaneously, has improved reaction rate greatly and has shortened reaction time.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a tower kettle reactor comprises a reactor body, wherein the reactor body comprises a reaction kettle and a reaction tower which is integrally connected to the top end of the reaction kettle, and the reaction kettle is provided with a main feed inlet; the reaction tower is internally provided with a corrugated carrier, a circulating flow guide device is arranged beside the reaction tower, and a liquid reactant enters the reaction kettle from the main feed inlet to reach a preset filling amount and is guided into the reaction tower by the circulating flow guide device to flow back to the reaction kettle from the upper part of the corrugated carrier; and a spraying pipe for spraying the vaporous reactants is arranged in the reaction kettle at a position close to the kettle bottom.
The volume of the reactor body for reaction is improved by the integral connection of the reaction kettle and the reaction tower, the production preparation amount can be improved, the main feed inlet can be used for leading in liquid reactants, and the arrangement of the blow-off pipe close to the kettle bottom ensures that the leading-in vapor reactants and the liquid reactants are subjected to primary reaction; meanwhile, the liquid reactant at the bottom of the reaction kettle is guided to the upper part of the corrugated carrier in the reaction tower by the circulating diversion device, the corrugated carrier can delay the falling speed and time of the liquid reactant, and the unreacted vapor reactant is fully contacted with the liquid reactant falling from the corrugated carrier in the upward moving process to carry out secondary reaction.
The downward flow of the liquid reactant and the upward flow of the vapor reactant in the reaction tower can cause the pressure difference between the inside of the reaction kettle and the upper part of the reaction tower; under the pressure difference, the temperature in the reactor at the bottom of the tower can be raised to more than 100 ℃, and the reaction rate is greatly improved.
Preferably, the height of the reactor body is 5-15m, the height of the reaction tower is 2-3 times of the height of the reaction kettle, and the cross-sectional area of the reaction kettle is 2-3 times of the cross-sectional area of the reaction tower.
The height of the reactor body is set to increase the reaction volume, and the height of the reaction tower is higher than that of the reaction kettle to increase the path length of the liquid reactant when the liquid reactant flows down from the top of the reaction tower under the guidance of the circulating flow guide device, so that the liquid reactant can be more fully contacted with the rising vapor reactant.
Preferably, the circulating flow guide device comprises a circulating pump and two guide pipes, and the circulating pump is respectively communicated with the bottom of the reaction kettle and the side wall of the reaction tower at corresponding positions above the corrugated carrier through the two guide pipes.
Preferably, the guide pipe is connected with the end of the side wall of the reaction tower at the corresponding position above the corrugated carrier, extends into the reaction tower and is connected with the spray head.
When liquid reactants are guided, the liquid reactants at the bottom of the reaction kettle are pumped to the upper part of the corrugated carrier in the reaction tower through the guide pipe by the pumping of the circulating pump, the liquid reactants can cover the upper part of the corrugated carrier by the spraying of the spray head, and the liquid reactants are in full contact reaction with the ascending vapor reactants in the falling process.
Preferably, the blowing pipe is fixed on the inner side wall of the reaction kettle and is immersed in the liquid reactant, and the blowing pipe is further provided with a plurality of inclined holes facing the axis direction of the middle part of the blowing pipe in the circumferential direction.
Preferably, the blow-off pipe is of a square structure, and the inclined holes are arranged on the opposite inner walls of the blow-off pipe.
Preferably, the blowing pipe is of a circular structure, the inclined hole is formed in the bottom of the blowing pipe, a plurality of pressure pipes with the diameter smaller than that of the blowing pipe are arranged at the inclined hole of the blowing pipe, and the end portions of the pressure pipes are further provided with bell mouths.
The effect of blowing pipe is in order to make things convenient for in the gaseous reactant of follow external guide, gaseous reactant accessible pressure boost pipe when being full of blowing pipe is to leading in the liquid reactant, the diameter of pressure boost pipe is less than blowing pipe, consequently pressure can the grow after getting into the pressure boost pipe during gaseous reactant, and then can stir when spouting and churn more liquid reactant, the setting of horn mouth also can contact more liquid reactant in order to make gaseous reactant when spouting out, thereby the reaction is more abundant and quick.
Compared with the prior art, the beneficial effects of the utility model are that:
1. the integrated arrangement of the reaction kettle and the reaction tower greatly improves the reaction volume, saves the occupied area, guides the liquid reactant into the reaction tower through the circulating flow guide device to fall and perform secondary reaction with the ascending vapor reactant, shortens the reaction time and improves the reaction efficiency, and the downward flow of the liquid reactant and the upward flow of the vapor reactant in the reaction tower can form pressure difference between the inside of the reaction kettle and the upper part of the reaction tower; under the pressure difference, the temperature in the tower reactor can be raised to more than 100 ℃, and the reaction rate is further improved.
2. Can carry out a plurality of times of reactions in the reaction kettle and the reaction tower, and the vapor-state reactant is stirred to turn over the liquid-state reactant to replace the traditional stirring mode, thereby further ensuring the full reaction.
The arrangement of the blow-off pipe also enables the vapor reactant to stir and tumble the liquid reactant to fully contact with the liquid reactant during the initial reaction, so that the reaction rate is improved.
Drawings
FIG. 1 is a schematic diagram of the structure of a reactor body in the present invention;
FIG. 2 is a schematic structural view of a blow-off pipe according to the present invention;
FIG. 3 is a front view of the discharge tube of the present invention;
fig. 4 is a schematic structural diagram of the medium filler carrier of the present invention.
Description of the drawings: 1. a reactor body; 101. a reaction kettle; 102. a reaction tower; 103. a main feed inlet; 2. a circulation pump; 201. a guide tube; 3. a blow-off pipe; 301. a pressure increasing pipe; 302. a bell mouth; 4. a corrugated carrier; 5. a spray head; 6. a storage tank; 7. a heater; 8. a condenser; 9. a dehydration separator; 10. and a defogging net.
Detailed Description
The following describes in detail an embodiment of the present invention with reference to the drawings.
In the embodiment, a tower reactor is specifically disclosed, as shown in fig. 1-4, the specific structure of the tower reactor comprises a reactor body 1, the reactor body 1 comprises a reaction kettle 101 and a reaction tower 102 integrally connected to the top end of the reaction kettle 101, and the reaction kettle 101 is provided with a main feed inlet 103; the corrugated carriers 4 are arranged in the reaction tower 102, the circulating guide device is also arranged beside the reaction tower 101, and liquid reactants enter the reaction kettle 101 from the main feed inlet 103 to reach a preset filling amount and are guided into the reaction tower 102 by the circulating guide device to flow from the upper part of the corrugated carriers 4 and fall back into the reaction kettle 101; and a spraying pipe 3 for spraying the vaporous reactants is arranged in the reaction kettle 101 and is close to the kettle bottom.
The conventional reaction has a small tank volume and is mixed by stirring, but the esterification reaction rate is slow, and the reactor body 1 in this embodiment is formed by integrating the reaction tower 102 on the reaction tank 101, the height of the reactor body 1 is 5-15m, the height of the reaction tower 102 is 2-3 times of the height of the reaction tank 101, and the cross-sectional area of the reaction tank 101 is 2-3 times of the cross-sectional area of the reaction tower 102. Not only the volume is increased, but also the traditional stirring mode of a stirring paddle is replaced by stirring the liquid reactant by adding the vapor reactant, so that the reaction is more sufficient through multiple reactions, and the energy consumption is also saved by stirring the vapor reactant. Wherein the height of the reaction tower 102 is greater than the height of the reaction vessel 101, so that the path through which the liquid reactant flows is longer, and thus the vapor reactant is more fully contacted.
In the following synthesis example of isopropyl palmitate, palmitic acid and isopropanol are thermally esterified to isopropyl palmitate under the catalysis of sulfuric acid, an azeotrope is a product formed by water and isopropanol generated in the esterification reaction, wherein the water content is 12.1% and the isopropanol content is 87.9%, and the product needs to be removed in the preparation process because the product has a certain influence on the conversion rate of reactants.
During production, after palmitic acid enters the reaction kettle 101 from the main feed inlet 103 to reach a preset addition amount, isopropanol reacting with the palmitic acid is heated and vaporized into a vaporous reactant from the stock chest 6 through the heater 7 before being introduced into the reaction kettle 101, and the vaporous reactant is introduced into the reaction kettle 101 through the blow-off pipe 3; in order to ensure that the vaporous reactant can be fully contacted with the palmitic acid, the blowing pipe 3 is arranged at the position of the reaction kettle 101 close to the kettle bottom to be immersed into the palmitic acid, so that the palmitic acid is surged to be fully contacted with the palmitic acid for primary reaction.
While the initial reaction is carried out, the circulating diversion device guides the palmitic acid in the reaction kettle 101 to the position above the corrugated carrier 6 in the reaction tower 102, and then the palmitic acid falls through the corrugated carrier 6, usually, in order to ensure that the palmitic acid can be completely reacted, excessive vaporous reactants are introduced, the vaporous reactants which are not reacted after the initial reaction rise through the corrugated carrier 6, and the corrugated carrier 6 can delay the falling speed and time of the liquid reactants, so that the vaporous reactants can be fully contacted with the vaporous reactants to carry out secondary reaction in the rising process. Meanwhile, the downward flow of palmitic acid and the upward flow of the vaporous reactant in the reaction tower 102 cause a pressure difference to be formed between the inside of the reaction kettle 101 and the upper part of the reaction tower 102; under the pressure difference, the temperature in the reactor body 1 can be raised to be more than 100 ℃, so that the reaction rate is greatly improved; the reaction time is greatly shortened for the existing production mode, which is 20-30% of the time.
The top of the reaction tower 102 is also provided with a demisting net 10, the esterification product generated after the reaction can be isolated by the demisting net 10, and the vaporous reactant and the azeotrope generated in the esterification reaction can be discharged from the outlet of the reaction tower 102 after passing through the demisting net 10.
The discharged vaporous reactant and azeotrope are introduced into a condenser 8 for condensation, a part of condensed reactant can be introduced into the top of the reaction tower 102, the temperature of the top is controlled to be 80.5 ℃, and the rest part of condensed reactant is continuously introduced into a dehydration separator 9 for dehydration treatment and then introduced into a storage tank 6 for recycling.
As shown in fig. 1, the circulation diversion apparatus includes a circulation pump 2 and two guide pipes 201, and the circulation pump 2 is respectively communicated with the bottom of the reaction kettle 101 and the side wall of the reaction tower 102 at corresponding positions above the corrugated carrier 6 through the two guide pipes 201.
The end of the guide pipe 201 connected to the side wall of the reaction tower 102 at the corresponding position above the corrugated carrier 6 extends into the reaction tower 102 and is connected with the spray head 7.
The process of guiding palmitic acid is as follows: the circulating pump 2 is pumped out through a guide pipe 201 communicated with the bottom of the reaction kettle 101 and then is pumped into the reaction tower 102, and the palmitic acid is sprayed onto the upper surface of the corrugated carrier 6 through the spray head 7, so that when the vaporous reactant enters the reaction kettle 101, a pressure difference is formed between the reaction tower 102 at the position of the corrugated carrier 6 and the top of the reaction kettle 101 and the top of the reaction tower 102, and the pressure difference between the position of the spray head 7 and the connection between the reaction kettle 101 and the reaction tower 102 is 0.025-0.075 MPa.
The blowing pipe 3 is fixed on the inner side wall of the reaction kettle 101 and is immersed into the liquid reactant, and the blowing pipe 3 is also provided with a plurality of inclined holes facing the axis direction of the middle part of the blowing pipe 3 in the circumferential direction.
The blow-off pipe 3 can be a square structure, and the inclined holes are arranged on the opposite inner walls of the blow-off pipe 3.
The inclined holes can enable the vaporous reactants to be sprayed into the palmitic acid in an inclined mode to form a palmitic acid stirring and overturning path as shown by L in figure 3, so that the two reactants can be mixed more uniformly and fully.
As shown in fig. 2-3, the blowing pipe 3 may also be a circular ring structure, the inclined hole is disposed at the bottom of the blowing pipe 3, a plurality of pressure increasing pipes 301 with a diameter smaller than that of the blowing pipe 3 are disposed at the inclined hole of the blowing pipe 3, and a bell mouth 302 is further disposed at an end of each pressure increasing pipe 301.
When the vaporous reactant is introduced into the palmitic acid, the vaporous reactant is sprayed through a pressurizing pipe 301 which is obliquely arranged on the spraying pipe 3, the liquid reactant is stirred and overturned to enable the reaction to be more sufficient and rapid, the stirring direction of the liquid reactant is shown in figure 3, and L in the figure is the stirring direction and the stirring path of the liquid reactant; the gaseous reactant is led into earlier in the blowing pipe 3 because the diameter of booster pipe 301 is less than blowing pipe 3, therefore when leading-in booster pipe 301, pressure can increase, forms the one-level steam column this moment, and the one-level steam column drives the palmitic acid in the bellmouth 302 earlier and stirs and form the second grade steam column, and the stirring to the liquid reactant is tumbled more violent when the second grade steam column is spouted out from bellmouth 302, and bellmouth 302 also can improve thereby stirs more liquid reactant with the area of contact of liquid reactant.
The above description of the present invention is intended to be illustrative. Various modifications, additions and substitutions may be made by those skilled in the art without departing from the scope of the invention as defined in the accompanying claims.
Claims (7)
1. A tower reactor comprises a reactor body (1), and is characterized in that the reactor body (1) comprises a reaction kettle (101) and a reaction tower (102) integrally connected to the top end of the reaction kettle (101), wherein the reaction kettle (101) is provided with a main feeding hole (103); the reaction tower (102) is internally provided with a corrugated carrier (4), a circulating flow guide device is also arranged beside the reaction tower (102), and liquid reactants enter the reaction kettle (101) from the main feed inlet (103) to reach a preset filling amount and are guided into the reaction tower (102) from the upper part of the corrugated carrier (4) by the circulating flow guide device and flow back into the reaction kettle (101); and a spraying pipe (3) for spraying the vaporous reactants is arranged in the reaction kettle (101) and is close to the kettle bottom.
2. The column bottom reactor according to claim 1, wherein the height of the reactor body (1) is 5-15m, the height of the reaction column (102) is 2-3 times the height of the reaction column (101), and the cross-sectional area of the reaction column (101) is 2-3 times the cross-sectional area of the reaction column (102).
3. The column bottom reactor according to claim 1, wherein the circulation diversion device comprises a circulation pump (2) and two guide pipes (201), and the circulation pump (2) is respectively communicated with the bottom of the reaction kettle (101) and the side wall of the reaction tower (102) at corresponding positions above the corrugated carrier (4) through the two guide pipes (201).
4. A column bottom reactor according to claim 3, characterized in that the end of the guide tube (201) connected to the side wall of the reaction column (102) at the corresponding position above the corrugated carrier (4) extends into the reaction column (102) and is connected to the spray head (5).
5. The column reactor according to claim 1, wherein the blow-off pipe (3) is fixed on the inner side wall of the reaction kettle (101) and is immersed in the liquid reactants, and the blow-off pipe (3) is further provided with a plurality of inclined holes facing the axial direction of the middle part of the blow-off pipe (3) in the circumferential direction.
6. The column bottom reactor according to claim 5, characterized in that the blow-off pipe (3) is of a square structure, and the inclined holes are arranged on the opposite inner walls of the blow-off pipe (3).
7. The tower kettle reactor according to claim 5, wherein the blow-off pipe (3) is of a circular ring structure, an inclined hole is arranged at the bottom of the blow-off pipe (3), the blow-off pipe (3) is provided with a plurality of pressure increasing pipes (301) with a diameter smaller than that of the blow-off pipe (3) at the inclined hole, and the end parts of the pressure increasing pipes (301) are further provided with bell mouths (302).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221207899.0U CN217288430U (en) | 2022-05-19 | 2022-05-19 | Tower kettle reactor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221207899.0U CN217288430U (en) | 2022-05-19 | 2022-05-19 | Tower kettle reactor |
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| CN217288430U true CN217288430U (en) | 2022-08-26 |
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| CN202221207899.0U Active CN217288430U (en) | 2022-05-19 | 2022-05-19 | Tower kettle reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253990A (en) * | 2022-05-19 | 2022-11-01 | 湖北赛恩利精细化工有限公司 | Production facility for esterification reaction |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115253990A (en) * | 2022-05-19 | 2022-11-01 | 湖北赛恩利精细化工有限公司 | Production facility for esterification reaction |
| CN115253990B (en) * | 2022-05-19 | 2024-03-26 | 湖北赛恩利精细化工有限公司 | Production equipment for esterification reaction |
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