Pre-reactor for producing 3, 4-dihydroxy-1-butene
By designing a 3,4-dihydroxy-1-butene production pre-reactor including a storage tank, a pressurized pump, a heat exchanger, a heater, a primary catalytic reactor and a secondary catalytic reactor, the problems of low reaction efficiency and high energy consumption in the prior art are solved, and more efficient catalytic reactions and heat recovery are achieved.
Patent Information
- Application Number
- CN202420388067.6
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-02-29
- Publication Date
- 2025-03-07
- Estimated Expiration
- 2034-02-28
AI Technical Summary
The existing isomerization reaction of 3,4-butene glycol requires continuous stirring to ensure the catalyst contacts with the reactants, resulting in low reaction efficiency and high energy consumption.
A 3,4-dihydroxy-1-butene production pre-reactor is designed, including a storage tank, a pressurized pump, a heat exchanger, a heater, a primary catalytic reactor and a secondary catalytic reactor, and continuous catalytic reaction and heat recovery are achieved through a series of reactors and heat exchangers.
Through continuous catalytic reaction and heat recovery, the reaction efficiency is improved, energy consumption is reduced, the use of stirring equipment is avoided, and a more efficient production process is achieved.
Smart Images
Figure CN222567707U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to chemical equipment, in particular to a pre-reactor for producing 3,4-dihydroxy-1-butene. Background Art
[0002] 3,4-Butenediol is an important organic intermediate and an important raw material for the synthesis of vinyl carbonate, an additive for lithium-ion batteries. It is mainly obtained by rearrangement of 1,4-butenediol by isomerization reaction under the catalysis of a catalyst. Most of the catalysts are solid and cannot be dissolved in 1,4-butenediol. Therefore, in the past, the reactor needed to be continuously stirred to make it contact with the powdered catalyst inside. This method has low reaction efficiency and very high energy consumption. Utility Model Content
[0003] The technical problem to be solved by the utility model is to provide a pre-reactor for producing 3,4-dihydroxy-1-butene, so as to solve the technical problem in the background technology.
[0004] In order to solve the above technical problems, the technical solution of the utility model is:
[0005] A 3,4-dihydroxy-1-butene production pre-reactor comprises a storage tank, a primary pressure pump, a heat exchanger, a heater, a primary catalytic reactor and a secondary catalytic reactor; the outlet of the storage tank is connected to a low-temperature water inlet of a heat exchanger through a water pipe A, and a primary heating pump is connected in series to the water pipe A; the high-temperature water outlet of the heat exchanger is connected in series with a heater, a primary catalytic reactor and a secondary catalytic reactor in sequence through a pipeline, the outlet of the secondary catalytic reactor is connected to the high-temperature water inlet of the heat exchanger through a water pipe B, and the low-temperature water outlet of the heat exchanger is connected to a discharge pipe.
[0006] Furthermore, the heater is a resistance wire tube heater.
[0007] Furthermore, a secondary pressure pump is connected in series between the primary catalytic reactor and the secondary catalytic reactor.
[0008] Furthermore, the heat exchanger is a shell and tube heat exchanger.
[0009] Furthermore, the primary catalytic reactor and the secondary catalytic reactor both include a shell, with an inlet and an outlet arranged at both ends of the shell, and metal foam fillers and microporous carriers are alternately arranged in the shell, and the catalyst is combined with the microporous carrier.
[0010] Furthermore, the catalyst is cuprous oxide or cuprous chloride.
[0011] Advantages of the utility model:
[0012] The utility model uses a primary catalytic reactor and a secondary catalytic reactor to carry out continuous catalytic reactions. The product is formed at one time, and all raw materials will react through them in sequence, thereby saving large-scale stirring equipment and greatly improving the time of the catalytic reaction. Moreover, the heating is carried out in sequence, and the heat is recovered through the heat exchanger. Compared with the reactor, the production efficiency is higher and the energy consumption is lower. BRIEF DESCRIPTION OF THE DRAWINGS
[0013] Figure 1 It is a schematic diagram of the structure of the utility model;
[0014] Figure 2 Schematic diagram of the primary catalytic reactor structure.
[0015] In the figure, 1-storage tank, 11-water pipe A, 2-primary pressure pump, 3-heat exchanger, 4-heater, 5-primary catalytic reactor, 5a-secondary catalytic reactor, 51-shell, 52-microporous carrier, 53-metal foam filler, 6-secondary pressure pump, 7-water pipe B, 8-discharge pipe. DETAILED DESCRIPTION
[0016] The specific implementation methods of the present invention are further described below in conjunction with the accompanying drawings. It should be noted that the description of these implementation methods is used to help understand the present invention, but does not constitute a limitation of the present invention. In addition, the technical features involved in each implementation method of the present invention described below can be combined with each other as long as they do not conflict with each other.
[0017] As shown in the figure:
[0018] A 3,4-dihydroxy-1-butene production pre-reactor comprises a storage tank 1, a primary pressure pump 2, a heat exchanger 3, a heater 4, a primary catalytic reactor 5 and a secondary catalytic reactor 5a; the outlet of the storage tank 1 is connected to the low-temperature water inlet of the heat exchanger 3 through a water pipe A11, and a primary heating pump is connected in series to the water pipe A11; the high-temperature water outlet of the heat exchanger 3 is connected in series with the heater 4, the primary catalytic reactor 5 and the secondary catalytic reactor 5a in sequence through a pipeline, the outlet of the secondary catalytic reactor 5a is connected to the high-temperature water inlet of the heat exchanger 3 through a water pipe B7, and the low-temperature water outlet of the heat exchanger 3 is connected to a discharge pipe 8.
[0019] Working principle: 1,4-butenediol to be catalytically reacted is stored in a storage tank 1, and then a booster pump 2 is started. When the 1,4-butenediol passes through the heater 4, it will be heated to 100 degrees Celsius to reach the temperature of the catalytic reaction, and then enters the primary catalytic reactor 5 and the secondary catalytic reactor 5a to be catalyzed by the catalyst therein. The length of the primary catalytic reactor 5 and the secondary catalytic reactor 5a can be extended according to the flow rate. If the pressure is insufficient, a secondary booster pump 6 is connected in series between the primary catalytic reactor 5 and the secondary catalytic reactor 5a.
[0020] In the primary catalytic reactor 5 and the secondary catalytic reactor 5a, 1,4-butenediol undergoes an isomerization reaction under the action of the catalyst to generate 3,4-dihydroxy-1-butene, and then the product at a higher temperature will enter the heat exchanger 3 to exchange heat with the raw material that is about to enter the heater 4 for heating, thereby recovering part of the heat to achieve the purpose of energy saving. The heat exchanger 3 is preferably a shell-and-tube heat exchanger 3, and the low-temperature raw material passes through the shell and tube, and the high-temperature product passes through the tank body.
[0021] Since the utility model adopts a continuous production method, the heater 4 is preferably a resistance wire tube heater 4, so that the temperature gradually increases from the inlet to the outlet of the heater 4 and reaches the pre-reaction temperature at the outlet.
[0022] In order to increase the catalytic efficiency, the primary catalytic reactor 5 and the secondary catalytic reactor 5a both include a shell 51, with an inlet and an outlet arranged at both ends of the shell 51, and metal foam fillers 53 and microporous carriers 52 are staggered in the shell 51. The microporous carrier 52 is combined with a catalyst. The gaps in the metal foam fillers 53 are staggered for unpowered mixing, and the microporous carrier 52 is processed with a number of parallel and penetrating fine channels. The channels are combined with catalysts to allow the raw materials to fully contact the catalyst, thereby improving the catalytic efficiency. The catalyst can be cuprous oxide or cuprous chloride.
[0023] The embodiments of the present invention are described in detail above with reference to the accompanying drawings, but the present invention is not limited to the described embodiments. For those skilled in the art, various changes, modifications, substitutions and variations of these embodiments are made without departing from the principles and spirit of the present invention, and still fall within the scope of protection of the present invention.
Claims
1. A pre-reactor for producing 3,4-dihydroxy-1-butene, characterized in that: It includes a storage tank, a primary pressure pump, a heat exchanger, a heater, a primary catalytic reactor and a secondary catalytic reactor; the outlet of the storage tank is connected to the low-temperature water inlet of the heat exchanger through a water pipe A, and a primary heating pump is connected in series to the water pipe A; the high-temperature water outlet of the heat exchanger is connected in series with the heater, the primary catalytic reactor and the secondary catalytic reactor in sequence through pipelines, the outlet of the secondary catalytic reactor is connected to the high-temperature water inlet of the heat exchanger through a water pipe B, and the low-temperature water outlet of the heat exchanger is connected to the discharge pipe.
2. The 3,4-dihydroxy-1-butene production pre-reactor according to claim 1, characterized in that: The heater is a resistance wire tube heater.
3. The 3,4-dihydroxy-1-butene production pre-reactor according to claim 1, characterized in that: A secondary pressure pump is connected in series between the primary catalytic reactor and the secondary catalytic reactor.
4. The 3,4-dihydroxy-1-butene production pre-reactor according to claim 2, characterized in that: The heat exchanger is a shell and tube heat exchanger.
5. The 3,4-dihydroxy-1-butene production pre-reactor according to any one of claims 1 to 4, characterized in that: The primary catalytic reactor and the secondary catalytic reactor both include a shell, with an inlet and an outlet arranged at both ends of the shell, and metal foam fillers and microporous carriers arranged alternately in the shell, and a catalyst is combined on the microporous carrier.
6. The 3,4-dihydroxy-1-butene production pre-reactor according to claim 5, characterized in that: The catalyst is cuprous oxide or cuprous chloride.