CN215693846U - Optimized hydrogenation reaction system - Google Patents
Optimized hydrogenation reaction system Download PDFInfo
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- CN215693846U CN215693846U CN202121667787.9U CN202121667787U CN215693846U CN 215693846 U CN215693846 U CN 215693846U CN 202121667787 U CN202121667787 U CN 202121667787U CN 215693846 U CN215693846 U CN 215693846U
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Abstract
The utility model provides an optimized hydrogenation reaction system, which comprises a tubular reactor, a first liquid separation tank, a condenser and a circulating hydrogen compressor, wherein a sampling port at the top of the tubular reactor is communicated with a maleic anhydride solvent sampling pipeline and a hydrogen gas sampling pipeline; a production pipeline on the side wall of the bottom of the tubular reactor is communicated with a first liquid separation tank, a circulating hydrogen return pipeline at the top of the first liquid separation tank is connected with a production inlet of a circulating hydrogen compressor, and a production outlet of the circulating hydrogen compressor is communicated with a hydrogen production pipeline; the side wall of the tubular reactor is connected with a hot water extraction pipeline and a hot water extraction pipeline; the bottom sampling port of the tubular reactor is connected with a liquid phase reaction product rectification system sampling pipeline, the utility model can be recycled, the energy consumption can be reduced by more than 30%, the one-way processing capacity is improved by 50-500%, the conversion rate reaches 90-100%, and the processing cost is greatly reduced.
Description
Technical Field
The utility model belongs to the field of hydrogenation reaction, and particularly relates to an optimized hydrogenation reaction system.
Background
The production of succinic anhydride (succinic anhydride), succinic acid (succinic acid), dimethyl succinate (dimethyl succinate) and diethyl succinate (diethyl succinate) by hydrogenation of raw materials is a commonly used method at present, the reaction system obtains a finished product after gas-liquid separation and recovers a separation solvent, the production efficiency can be effectively improved, but the hydrogenation reaction is a strong exothermic reaction, the adiabatic temperature rise of the reaction is very large, the reaction energy consumption is high, no heat removal means is included, and the exothermic effect in the hydrogenation reaction system cannot be effectively solved.
In the prior art, a fixed bed reactor without heat removal measures is adopted, the raw materials are diluted by a solvent, the concentration of the raw materials is controlled in a lower range, and a large amount of circulating solvent carries heat to control the temperature rise of a reaction bed layer, so that the occurrence of side reactions is inhibited. The recycled solvent needs to be separated from the rectification system and then returned to the reaction system, and a large amount of energy is consumed. In addition, the lower concentration of raw materials limits the processing capacity of the reaction system, and how to adopt effective means to reduce the strong exothermic effect of the reaction is a difficult point to solve.
Disclosure of Invention
In view of the above, the present invention aims to provide an optimized hydrogenation reaction system, in which a shell and tube reactor is adopted, a gas-liquid distribution assembly is arranged in the shell and tube reactor, and a multi-point thermometer is arranged in a heat exchange tube of the shell and tube reactor, so as to overcome the defects that the reaction heat release is large, the heat transfer is not easy, and the energy consumption of the heat transfer method is high in the prior art.
In order to achieve the purpose, the technical scheme of the utility model is realized as follows:
an optimized hydrogenation reaction system comprises a tubular reactor, a first liquid separation tank, a condenser and a circulating hydrogen compressor, wherein the top of the tubular reactor is connected with a raw material sampling pipeline;
the side wall of the bottom of the tubular reactor is communicated with the first liquid separation tank through a pipeline, and the condenser is positioned on the pipeline between the side wall of the bottom of the tubular reactor and the first liquid separation tank; the top of the first liquid separation tank is connected with a hydrogen gas extraction pipeline through a pipeline, the hydrogen gas extraction pipeline is communicated with a raw material extraction pipeline, and a circulating hydrogen compressor is positioned on the hydrogen gas extraction pipeline;
the side wall of the tubular reactor is connected with a hot water extraction pipeline and a hot water extraction pipeline;
the bottom of the tubular reactor is connected with a first liquid phase product extraction pipeline.
Furthermore, a condensate liquid extraction pipeline is connected to an extraction outlet at the bottom of the first liquid separation tank and communicated with the first liquid-phase product extraction pipeline.
Furthermore, the top of the first liquid separation tank is connected with a circulating hydrogen return pipeline, and the circulating hydrogen return pipeline is connected with a new hydrogen intake pipeline.
Furthermore, a multi-point thermometer is arranged in the heat exchange tube of the tube type reactor.
The shell pass of the tubular reactor adopts forced circulation hot water to take out heat released in the hydrogenation reaction process, and the stability of the reaction temperature in the heat exchange tube is kept.
The multi-point thermometer is arranged in the heat exchange tube of the tubular reactor and used for detecting the central temperature of the heat exchange tube of the tubular reactor.
The system further comprises a secondary reactor and a second liquid separation tank, wherein the top of the secondary reactor is communicated with the second liquid separation tank through a pipeline, the bottom of the second liquid separation tank is connected with a second liquid-phase product extraction pipeline, and the top of the second liquid separation tank is communicated with a circulating hydrogen compressor through a circulating hydrogen pipeline.
Furthermore, an interstage booster pump is connected to the first liquid-phase product extraction pipeline and connected with the bottom of the secondary reactor through a pipeline.
Furthermore, the hydrogen gas intake pipeline is divided into two branches, one branch is connected with the raw material intake pipeline, and the other branch is connected with the bottom side wall of the secondary reactor.
Further, the second liquid-phase product extraction pipeline is communicated with a rectification system.
Further, a gas-liquid distribution assembly is arranged in the shell and tube reactor.
The raw material is one of maleic anhydride (maleic anhydride and maleic anhydride), maleic acid (maleic acid and maleic acid), dimethyl maleate (dimethyl maleate and dimethyl maleate) and diethyl maleate (diethyl maleate and diethyl maleate); the product of the utility model is one of succinic anhydride (succinic anhydride), succinic acid (succinic acid), dimethyl succinate (dimethyl succinate) and diethyl succinate (diethyl succinate).
The reaction system is suitable for preparing succinic anhydride by maleic anhydride hydrogenation, succinic acid by maleic acid hydrogenation, dimethyl succinate by dimethyl maleate and diethyl succinate by diethyl maleate hydrogenation.
Compared with the prior art, the utility model has the beneficial effects that:
according to the utility model, a tubular reactor convenient for heat removal is adopted in a hydrogenation reaction system, hot water is introduced into the tubular reactor and extracted to take out heat, hydrogen in a gas-phase product is cooled by a condenser and then enters a circulating hydrogen compressor again through a return line, the hydrogen can be recycled, the energy consumption can be reduced by more than 30% by using the system, the one-way treatment capacity is improved by 50% -500%, the conversion rate reaches 90-100%, and the processing cost is greatly reduced.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate an embodiment of the utility model and, together with the description, serve to explain the utility model and not to limit the utility model.
In the drawings:
FIG. 1 is a schematic diagram of a reaction system for preparing succinic anhydride by hydrogenation of maleic anhydride according to example 1 of the present invention;
FIG. 2 is a schematic diagram of a reaction system for preparing succinic anhydride by hydrogenation of maleic anhydride according to example 2 of the present invention;
description of reference numerals:
1-a tubular reactor; 2-a first liquid separation tank; 3-a condenser; 4-a recycle hydrogen compressor; 5-a secondary reactor; 6-a second liquid separation tank; and 7-interstage booster pump.
Detailed Description
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention. Furthermore, the terms "first", "second", etc. are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first," "second," etc. may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless otherwise specified.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art through specific situations.
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings.
Example 1
Maleic anhydride and a gamma-butyrolactone solvent are mixed according to a certain proportion, added into a raw material storage tank, fully stirred and dissolved to obtain a maleic anhydride raw material with higher concentration, the maleic anhydride raw material and hydrogen are fed into a tubular reactor 1 from the top of the tubular reactor 1, the side wall of the tubular reactor 1 is connected with a hot water inlet pipeline and a hot water outlet pipeline, the hot water inlet temperature is 60-80 ℃, the hot water return temperature is 90-130 ℃, the circulation volume of the hot water is determined according to the selection of the parameters, and the shell pass of the tubular reactor 1 adopts forced circulating hot water to take out heat released in the hydrogenation reaction process, so that the stability of the reaction temperature in a heat exchange tube is maintained.
The tubular reactor 1 is internally provided with a necessary gas-liquid distribution component, the concentration of maleic anhydride in reaction feed is 10-50%, the molar ratio of hydrogen at the inlet of the tubular reactor 1 to the maleic anhydride is 2-20, a multi-point thermometer is arranged in a heat exchange tube of the tubular reactor 1 and is used for detecting the central temperature of the heat exchange tube of the tubular reactor 1, a nickel catalyst is adopted as a catalyst filled in the tubular reactor 1, a maleic anhydride raw material and hydrogen are mixed and enter the heat exchange tube of the tubular reactor 1 for reaction, the reaction pressure of the reaction is 2-12MPaG, and the reaction temperature is 50-250 ℃.
The reacted material falls into the lower space of the tube pass of the reactor, the gas-liquid phase after the reaction is primarily separated, the gas phase carrying with a certain amount of liquid foam is extracted from the side wall of the tubular reactor 1, cooled and condensed by a condenser 3, and then separated from the liquid phase by a first liquid separation tank 2, the gas phase is taken as the circulating hydrogen and fresh hydrogen to be sent to a circulating hydrogen compressor 4, and the gas phase is pressurized and then returned to the upper inlet of the tubular reactor 1. The liquid phase of the first liquid separation tank 2 is converged with the liquid phase reaction product at the bottom of the tubular reactor 1 and sent to a rectification system together for product refining.
By using the reaction system of the embodiment 1, in the process of preparing succinic anhydride from maleic anhydride, the reaction energy consumption is reduced by more than 30%, the single-pass treatment capacity is improved by 50-500%, the conversion rate can reach more than 99%, and as the reaction system reduces the circulation amount of the solvent, the heat generated in the reaction process is taken away by hot water, so that the reaction system can be used for other purposes, and the processing cost is reduced.
Example 2
Maleic anhydride and a gamma-butyrolactone solvent are mixed according to a certain proportion, added into a raw material storage tank, fully stirred and dissolved to obtain a maleic anhydride raw material with higher concentration, the maleic anhydride raw material and hydrogen are fed into a tubular reactor 1 from the top of the tubular reactor 1, the side wall of the tubular reactor 1 is connected with a hot water inlet pipeline and a hot water outlet pipeline, the hot water inlet temperature is 60-80 ℃, the hot water return temperature is 90-130 ℃, the circulation volume of the hot water is determined according to the selection of the parameters, and the shell pass of the tubular reactor 1 adopts forced circulating hot water to take out heat released in the hydrogenation reaction process, so that the stability of the reaction temperature in a heat exchange tube is maintained.
The tubular reactor 1 is internally provided with a necessary gas-liquid distribution component, the concentration of maleic anhydride in reaction feed is 10-50%, the molar ratio of hydrogen at the inlet of the tubular reactor 1 to the maleic anhydride is 2-20, a multi-point thermometer is arranged in a heat exchange tube of the tubular reactor 1 and is used for detecting the central temperature of the heat exchange tube of the tubular reactor 1, a nickel catalyst is adopted as a catalyst filled in the tubular reactor 1, a maleic anhydride raw material and hydrogen are mixed and enter the heat exchange tube of the tubular reactor 1 for reaction, the reaction pressure of the reaction is 2-12MPaG, and the reaction temperature is 50-250 ℃.
The reacted material falls into the lower space of the tube pass of the reactor, the gas-liquid phase after the reaction is primarily separated, the gas phase carrying with a certain amount of liquid foam is extracted from the side wall of the tubular reactor 1, cooled and condensed by a condenser 3, and then separated from the liquid phase by a first liquid separation tank 2, the gas phase is taken as the circulating hydrogen and fresh hydrogen to be sent to a circulating hydrogen compressor 4, and the gas phase is pressurized and then returned to the upper inlet of the tubular reactor 1. The liquid phase of the first liquid separation tank 2 is merged with the liquid phase reaction product at the bottom of the tubular reactor 1, and is sent to an interstage booster pump 7, and enters the second reactor 1 from the bottom of the second reactor 1 after being boosted.
The hydrogen gas intake pipeline of the hydrogen gas compressor 4 is divided into two branches, one branch is connected with the raw material intake pipeline, the other branch is connected with the bottom side wall of the secondary reactor 5, the hydrogen gas and a liquid phase reaction product from the first liquid separation tank 2 and the bottom of the tubular reactor 1 continuously react, the reaction pressure of the reaction is 2-12MPaG, the reaction temperature is 50-250 ℃, a gas phase product after the reaction is extracted from the top of the second reactor 5 and enters the second liquid separation tank 6 for gas-liquid separation, the hydrogen gas is extracted from the top of the second liquid separation tank 6 and flows back to the circulating hydrogen compressor 4 through the circulating hydrogen pipeline to participate in the reaction again, and the liquid phase reaction product is extracted from the bottom of the second liquid separation tank 6 and enters the rectification system for product refining.
By using the reaction system of the embodiment 2, in the process of preparing succinic anhydride from maleic anhydride, the reaction energy consumption is reduced by more than 30%, the single-pass treatment capacity is improved by 50-500%, the conversion rate is close to 100%, and as the reaction system reduces the circulation amount of the solvent, the heat generated in the reaction process is taken away by hot water, so that the method can be used for other purposes, and the processing cost is reduced.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (9)
1. An optimized hydrogenation reaction system, which is characterized in that: the system comprises a tubular reactor (1), a first liquid separation tank (2), a condenser (3) and a circulating hydrogen compressor (4), wherein the top of the tubular reactor (1) is connected with a raw material sampling pipeline;
the side wall of the bottom of the tubular reactor (1) is communicated with the first liquid separation tank (2) through a pipeline, and the condenser (3) is positioned on the pipeline between the side wall of the bottom of the tubular reactor (1) and the first liquid separation tank (2); the top of the first liquid separation tank (2) is connected with a hydrogen gas extraction pipeline through a pipeline, the hydrogen gas extraction pipeline is communicated with a raw material extraction pipeline, and a circulating hydrogen compressor (4) is positioned on the hydrogen gas extraction pipeline;
the side wall of the tubular reactor (1) is connected with a hot water intake pipeline and a hot water intake pipeline;
the bottom of the tubular reactor (1) is connected with a first liquid phase product extraction pipeline.
2. An optimized hydrogenation reaction system according to claim 1, wherein: and a bottom extraction port of the first liquid separation tank (2) is connected with a condensation liquid extraction pipeline, and the condensation liquid extraction pipeline is communicated with a first liquid-phase product extraction pipeline.
3. An optimized hydrogenation reaction system according to claim 1, wherein: the top of the first liquid separation tank (2) is connected with a circulating hydrogen return pipeline, and the circulating hydrogen return pipeline is connected with a new hydrogen intake pipeline.
4. An optimized hydrogenation reaction system according to claim 1, wherein: and a multi-point thermometer is arranged in the heat exchange tube of the tube type reactor (1).
5. An optimized hydrogenation reaction system according to claim 1, wherein: a gas-liquid distribution component is arranged in the tubular reactor (1).
6. An optimized hydrogenation reaction system according to any one of claims 1-5, wherein: the system is characterized by further comprising a secondary reactor (5) and a second liquid separation tank (6), wherein the top of the secondary reactor (5) is communicated with the second liquid separation tank (6) through a pipeline, the bottom of the second liquid separation tank (6) is connected with a second liquid-phase product extraction pipeline, and the top of the second liquid separation tank (6) is communicated with a circulating hydrogen compressor through a circulating hydrogen pipeline.
7. An optimized hydrogenation reaction system according to claim 6, wherein: an interstage booster pump (7) is connected to the first liquid-phase product extraction and discharge pipeline, and the interstage booster pump (7) is connected with the bottom of the secondary reactor (5) through a pipeline.
8. An optimized hydrogenation reaction system according to claim 6, wherein: the hydrogen gas intake pipeline is divided into two branches, one branch is connected with the raw material intake pipeline, and the other branch is connected with the bottom side wall of the secondary reactor (5).
9. An optimized hydrogenation reaction system according to claim 6, wherein: and the second liquid-phase product extraction pipeline is communicated with the rectification system.
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| CN202121667787.9U CN215693846U (en) | 2021-07-21 | 2021-07-21 | Optimized hydrogenation reaction system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114682171A (en) * | 2022-04-15 | 2022-07-01 | 北京海望氢能科技有限公司 | High-efficiency dehydrogenation or hydrogenation reactor and dehydrogenation or hydrogenation process system for organic liquid |
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