CN215611599U - Reaction system for continuously producing tromethamine - Google Patents
Reaction system for continuously producing tromethamine Download PDFInfo
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- CN215611599U CN215611599U CN202121684921.6U CN202121684921U CN215611599U CN 215611599 U CN215611599 U CN 215611599U CN 202121684921 U CN202121684921 U CN 202121684921U CN 215611599 U CN215611599 U CN 215611599U
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Abstract
The technical problem to be solved by the utility model is to provide a reaction system for continuously producing tromethamine, which realizes continuous condensation reaction and hydrogenation reaction and ensures the continuity of working procedures, and comprises a continuous condensation reactor, a nitromethane feeding main pipe, a paraformaldehyde feeding pipe and a continuous hydrogenation reactor; the continuous condensation reactor comprises a plurality of reaction chambers which are sequentially communicated and distributed from top to bottom, wherein the side wall of each reaction chamber is provided with a nitromethane feeding hole and a circulating liquid outlet, the bottom of each reaction chamber is provided with a circulating liquid inlet, the outlet of a circulating pump I corresponding to the bottommost reaction chamber is respectively communicated with the feeding holes of a heat exchanger I and a continuous hydrogenation reactor through a three-way pipe, the lower part of the side wall of the continuous hydrogenation reactor is provided with a hydrogen inlet, the bottom of the continuous hydrogenation reactor is sequentially communicated with a circulating pump II and a heat exchanger II through pipelines, and the outlet of the heat exchanger II is communicated with the top of the continuous hydrogenation reactor.
Description
Technical Field
The utility model relates to the field of chemical equipment, in particular to a reaction system for continuously producing tromethamine.
Background
Tromethamine is also called tris (hydroxymethyl) aminomethane, is widely applied to acute metabolic and respiratory acidemia, is an alkaline buffer, and has good buffering effect on metabolic acidosis and enzyme activation reaction. In the existing synthesis process, a jacketed stirred tank reactor is generally used, cooling water is introduced into a jacket, and the reaction temperature is removed for controlling the reaction temperature. The adoption presss from both sides the cover stirred tank, can only intermittent operation, the material need be in the cauldron of difference material transfer, rise repeatedly and fall to press, intensity of labour is big, and the energy consumption is high, and the security is low and the device scale is restricted.
SUMMERY OF THE UTILITY MODEL
The technical problem to be solved by the utility model is to provide a reaction system for continuously producing tromethamine, which realizes continuous condensation reaction and hydrogenation reaction and ensures the continuity of working procedures.
The utility model is realized by the following technical scheme:
a reaction system for continuously producing tromethamine comprises a continuous condensation reactor, a nitromethane feeding main pipe, a paraformaldehyde feeding pipe and a continuous hydrogenation reactor;
the continuous condensation reactor comprises a plurality of reaction chambers which are sequentially communicated and distributed from top to bottom, the side wall of each reaction chamber is provided with a nitromethane feeding hole and a circulating liquid outlet, the bottom of each reaction chamber is provided with a circulating liquid inlet, the circulating liquid outlet is sequentially connected with a circulating pump I and a heat exchanger I through pipelines, and the outlet of the heat exchanger I is communicated with the circulating liquid inlet through a pipeline;
the top end of the reaction chamber at the top is provided with a total paraformaldehyde feed inlet, the paraformaldehyde feed pipe is communicated with the total paraformaldehyde feed inlet, and the nitromethane feed header is connected with all the nitromethane feed inlets in parallel;
the outlet of a circulating pump I corresponding to the bottommost reaction chamber is respectively communicated with the feed inlets of the heat exchanger I and the continuous hydrogenation reactor through a three-way pipe, the lower part of the side wall of the continuous hydrogenation reactor is provided with a hydrogen inlet, the bottom of the continuous hydrogenation reactor is sequentially communicated with a circulating pump II and a heat exchanger II through a pipeline, and the outlet of the heat exchanger II is communicated with the top of the continuous hydrogenation reactor.
Furthermore, in the continuous condensation reactor, except the bottommost reaction chamber, the side walls of the rest reaction chambers are provided with overflow outlets close to the top end; except the reaction chamber at the top, overflow liquid inlets are arranged at the positions of the side walls of the other reaction chambers close to the bottom; and between two adjacent reaction chambers, the overflow outlet of the reaction chamber positioned above is communicated with the overflow liquid inlet of the reaction chamber positioned below.
Further, the top of the reaction chamber is provided with a gas phase outlet, and the rest reaction chambers except the reaction chamber at the bottommost part are provided with gas phase inlets; between two adjacent reaction chambers, the gas phase inlet of the reaction chamber positioned above is communicated with the gas phase outlet of the reaction chamber positioned below.
Further, a catalyst pipeline is further arranged on a pipeline of the outlet of the heat exchanger II, which is communicated with the continuous hydrogenation reactor.
Further, the number of the reaction chambers is 3-6.
Compared with the prior art, the utility model has the following beneficial effects:
1. firstly, adding a certain amount of paraformaldehyde and nitromethane into the topmost reaction chamber through a total paraformaldehyde feed port and a nitromethane feed port for reacting for a period of time, then continuously adding the paraformaldehyde and the nitromethane, enabling liquid in the reaction chamber to enter the next reaction chamber through an overflow outlet, simultaneously adding a certain amount of nitromethane into the nitromethane feed port of the reaction chamber for reacting, and repeating the steps until all the reaction chambers have materials for reacting; liquid in each reaction chamber is subjected to heat exchange through a circulating liquid outlet and a heat exchanger I under the action of a circulating pump, and then enters the reaction chambers through a circulating liquid inlet, so that uninterrupted temperature control can be realized; finally, the materials in the bottommost reaction chamber react relatively thoroughly to meet the production requirement, then under the action of a circulating pump I, part of the reaction materials continuously enter a heat exchanger I for heat exchange and then return to the reaction chamber, and the other part of the reaction materials are continuously extracted and enter a continuous hydrogenation reactor for reaction with hydrogen;
the utility model can be operated continuously, control the temperature synchronously, reduce the labor intensity, improve the quality of the products;
2. the overflow outlet of the reaction chamber positioned above is communicated with the overflow liquid inlet of the reaction chamber positioned below, so that the reaction materials can be sequentially injected from top to bottom in the reaction chamber, and the continuity of charging is realized.
Drawings
FIG. 1 is a schematic diagram of the reaction system for continuously producing tromethamine according to the present invention;
FIG. 2 is a schematic view of the upper and middle reaction chambers of the present invention;
in the figure: 1. nitromethane feeding main pipe, 2, paraformaldehyde inlet pipe, 3, continuous hydrogenation ware, 4, go up the reacting chamber, 41, nitromethane feed inlet, 42, circulation liquid export, 43, circulation liquid import, 44, paraformaldehyde total feed inlet, 45, overflow outlet, 5, well reacting chamber, 51, overflow liquid import, 6, lower reacting chamber, 7, circulating pump I, 8, heat exchanger I, 9, circulating pump II, 10, heat exchanger II.
Detailed Description
The technical solutions in the embodiments of the present application will be described clearly and completely with reference to the drawings in the embodiments of the present application, and it is obvious that the described embodiments are only a part of the embodiments of the present application, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments of the present application without making any creative effort, shall fall within the protection scope of the present application.
In the description of the present invention, it is to be understood that the terms "upper", "lower", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience in describing the present invention and simplifying the description, but do not indicate or imply that the indicated device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus should not be construed as limiting the present invention.
As shown in fig. 1, the present embodiment discloses a reaction system for continuously producing tromethamine, which mainly comprises a continuous condensation reactor, a nitromethane feeding main pipe 1, a paraformaldehyde feeding pipe 2 and a continuous hydrogenation reactor 3.
Wherein, the continuous condensation reactor is composed of three reaction chambers, the three reaction chambers are distributed from top to bottom, and for convenience of description, the three reaction chambers are defined as an upper reaction chamber 4, a middle reaction chamber 5 and a lower reaction chamber 6 from top to bottom. As shown in figure 2, the side wall of each reaction chamber is provided with a nitromethane feeding hole 41, a circulating liquid outlet 42, and a circulating liquid inlet 43 is formed in the bottom of each reaction chamber, the circulating liquid outlet 42 is sequentially connected with a circulating pump I7 and a heat exchanger I8 through pipelines, and the outlet of the heat exchanger I8 is communicated with the circulating liquid inlet 43 through a pipeline.
The top end of the upper reaction chamber 4 is provided with a paraformaldehyde main feed port 44, and the side walls of the upper reaction chamber 4 and the middle reaction chamber 5 are provided with overflow outlets 45 near the top ends. The side walls of the middle reaction chamber 5 and the lower reaction chamber 6 are provided with overflow liquid inlets 51 near the bottom, the overflow outlet 45 of the upper reaction chamber 4 is communicated with the overflow liquid inlet 51 of the middle reaction chamber 5 through a pipeline, and the overflow outlet 45 of the middle reaction chamber 5 is communicated with the overflow liquid inlet 51 of the lower reaction chamber 6 through a pipeline. By the design, when the material in the upper reaction chamber 4 exceeds the overflow outlet 45, the material can enter the overflow liquid inlet 51 of the middle reaction chamber 5, so that the material in the middle reaction chamber 5 can be added, and when the material exceeds the overflow outlet 45 of the middle reaction chamber 5, the material can enter the overflow liquid inlet 51 of the lower reaction chamber 6, so that the continuous feeding of the three reaction chambers can be realized. Be equipped with the gaseous phase export at the top of every reaction chamber, go up reaction chamber 4 and the lateral wall of well reaction chamber 5 and be equipped with the gaseous phase import, the gaseous phase import of reaction chamber 5 in the gaseous phase export intercommunication of reaction chamber 6 under the messenger, the gaseous phase import of reaction chamber 4 in the gaseous phase export intercommunication of reaction chamber 5 in the messenger, so design, can use the noncondensable gas in each reaction chamber to up discharge in proper order, avoid noncondensable gas gathering in the reaction chamber to lead to the pressure too high to take place danger.
The paraformaldehyde feeding pipe 2 is communicated with a main paraformaldehyde feeding hole 44, the nitromethane feeding main pipe 1 is connected with all the nitromethane feeding holes 41 in parallel, and an outlet of a circulating pump I7 corresponding to the lower reaction chamber 6 is respectively communicated with the feeding holes of the heat exchanger I8 and the continuous hydrogenation reactor 3 through a three-way pipe. As the reaction in the lower material reaction chamber 6 is basically complete, the material can be introduced into the continuous hydrogenation reactor 3, and the reaction temperature is controlled by the heat exchanger I8. The lower part of the side wall of the continuous hydrogenation reactor 3 is provided with a hydrogen inlet, the bottom of the continuous hydrogenation reactor 3 is sequentially communicated with a circulating pump II 9 and a heat exchanger II 10 through pipelines, the outlet of the heat exchanger II 10 is communicated with the top of the continuous hydrogenation reactor 3, and the heat exchanger II 10 is used for removing reaction heat generated by hydrogenation reaction and maintaining the reaction temperature.
In this embodiment, the continuous hydrogenation reactor is a very important device in organic chemistry laboratories and in actual production processes, and not only can be used as a container for hydrogenation reaction, but also can be used in situations where liquid and gas need to be mixed sufficiently, and has wide application in the chemical pharmacy field, and can be used as basic equipment for product development, organic chemicals and pharmaceutical research, and can also be used for quantitative analysis of catalyst activity in industrial processes, and can be used in gas phase continuous hydrogenation processes, such as cyclohexane preparation by benzene atmospheric pressure gas phase hydrogenation, methanol synthesis by carbon monoxide high pressure gas phase hydrogenation, and the type of the reactor can be a tube type or a tower type.
The reaction system of the utility model has the following specific working process:
firstly, adding a certain amount of paraformaldehyde and nitromethane into the topmost reaction chamber through a total paraformaldehyde feed inlet and a nitromethane feed inlet to react for a period of time, and then continuously adding the paraformaldehyde and the nitromethane; liquid in the reaction chamber enters the next reaction chamber through the overflow outlet, a certain amount of nitromethane is added through the nitromethane feeding hole of the reaction chamber for reaction, and the like is repeated until all the reaction chambers have materials for reaction; liquid in each reaction chamber is subjected to heat exchange through a circulating liquid outlet and a heat exchanger I under the action of a circulating pump, and then enters the reaction chambers through a circulating liquid inlet, so that uninterrupted temperature control can be realized; and finally, the materials in the bottommost reaction chamber react relatively thoroughly to meet the production requirement, then under the action of the circulating pump I, one part of the reaction materials continuously enter the heat exchanger I for heat exchange and then return to the reaction chamber, the other part of the reaction materials are continuously extracted and enter the continuous hydrogenation reactor for reaction with hydrogen, and the heat exchanger II is used for removing the reaction heat generated by the hydrogenation reaction and maintaining the reaction temperature. And a catalyst pipeline is also arranged on a pipeline communicated with the continuous hydrogenation reactor at the outlet of the heat exchanger II, so that the catalyst and the cooled reaction liquid can enter the continuous hydrogenation reactor again. And a discharge pipe is communicated with the pipeline between the circulating pump II and the heat exchanger II through a three-way pipe, and part of reaction products can be discharged. The utility model can continuously operate, synchronously control the temperature, reduce the labor intensity and improve the product quality.
Claims (5)
1. A reaction system for continuously producing tromethamine is characterized by comprising a continuous condensation reactor, a nitromethane feeding main pipe, a paraformaldehyde feeding pipe and a continuous hydrogenation reactor;
the continuous condensation reactor comprises a plurality of reaction chambers which are sequentially communicated and distributed from top to bottom, the side wall of each reaction chamber is provided with a nitromethane feeding hole and a circulating liquid outlet, the bottom of each reaction chamber is provided with a circulating liquid inlet, the circulating liquid outlet is sequentially connected with a circulating pump I and a heat exchanger I through pipelines, and the outlet of the heat exchanger I is communicated with the circulating liquid inlet through a pipeline;
the top end of the reaction chamber at the top is provided with a total paraformaldehyde feed inlet, the paraformaldehyde feed pipe is communicated with the total paraformaldehyde feed inlet, and the nitromethane feed header is connected with all the nitromethane feed inlets in parallel;
the outlet of a circulating pump I corresponding to the bottommost reaction chamber is respectively communicated with the feed inlets of the heat exchanger I and the continuous hydrogenation reactor through a three-way pipe, the lower part of the side wall of the continuous hydrogenation reactor is provided with a hydrogen inlet, the bottom of the continuous hydrogenation reactor is sequentially communicated with a circulating pump II and a heat exchanger II through a pipeline, and the outlet of the heat exchanger II is communicated with the top of the continuous hydrogenation reactor.
2. The reaction system according to claim 1, wherein in the continuous condensation reactor, except for the bottommost reaction chamber, the side walls of the remaining reaction chambers are provided with overflow outlets at positions close to the top ends; except the reaction chamber at the top, overflow liquid inlets are arranged at the positions of the side walls of the other reaction chambers close to the bottom; and between two adjacent reaction chambers, the overflow outlet of the reaction chamber positioned above is communicated with the overflow liquid inlet of the reaction chamber positioned below.
3. The reaction system of claim 2, wherein the top of the reaction chamber is provided with a gas phase outlet, and the rest of the reaction chambers except the bottommost reaction chamber are provided with gas phase inlets; between two adjacent reaction chambers, the gas phase inlet of the reaction chamber positioned above is communicated with the gas phase outlet of the reaction chamber positioned below.
4. The reaction system according to claim 3, wherein a catalyst pipeline is further arranged on a pipeline of the outlet of the heat exchanger II communicated with the continuous hydrogenation reactor.
5. A reaction system according to any one of claims 1 to 4, wherein the number of reaction chambers is 3 to 6.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121684921.6U CN215611599U (en) | 2021-07-23 | 2021-07-23 | Reaction system for continuously producing tromethamine |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202121684921.6U CN215611599U (en) | 2021-07-23 | 2021-07-23 | Reaction system for continuously producing tromethamine |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114160053A (en) * | 2022-02-14 | 2022-03-11 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114160053A (en) * | 2022-02-14 | 2022-03-11 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
| CN114160053B (en) * | 2022-02-14 | 2022-05-31 | 龙口市化工厂 | Sulfuryl fluoride reaction device |
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