Neopentyl glycol production device
By immobilizing the catalyst in a neopentyl glycol production device, increasing the contact area with the reactants and optimizing the reaction conditions, the problem of insufficient contact between the catalyst and the reactants is solved, the catalytic reaction efficiency and the service life of the catalyst are improved, and the production effect with high conversion is achieved.
Patent Information
- Application Number
- CN202421835589.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-07-31
- Publication Date
- 2025-05-23
- Estimated Expiration
- 2034-07-31
AI Technical Summary
In the existing neopentyl glycol production equipment, the catalyst contact with the reactants is insufficient, resulting in low catalytic reaction efficiency and short service life of the catalyst, which requires frequent recycling and treatment.
A neopentyl glycol production device is designed, including reactor one and reactor two. A high-pressure mixing chamber, a catalyst bed and a heat exchanger are installed inside the reactor two. A liquid distributor, a catalyst fixed bed and jacket are installed inside the reactor two. The catalyst is fixed through these structures, increasing the contact area with the reactor, and optimizing the reaction conditions.
By immobilizing the catalyst, the efficiency of the catalytic reaction is improved, the service life of the catalyst is extended, and the operation of catalyst recovery and separation treatment is reduced. The conversion rate of hydroxyl phenanthaldehyde is increased to more than 99%.
Smart Images
Figure CN222889790U_ABST
Abstract
Description
Technical Field
[0001] The utility model belongs to the technical field of compound preparation, and specifically relates to a neopentyl glycol production device. Background Art
[0002] Neopentyl glycol is an important raw material for chemical production, has good chemical properties, and can participate in a variety of chemical reactions. At present, catalytic hydrogenation is usually used to prepare neopentyl glycol. Hydroxypivalaldehyde is used as a raw material, and a reduction reaction is carried out with hydrogen under high pressure conditions under the action of a catalyst to obtain neopentyl glycol. The catalytic hydrogenation reaction is usually carried out in a hydrogenation reactor.
[0003] Hydrogenation reactors have the advantages of high temperature resistance, corrosion resistance, and high production capacity, and are widely used in catalytic reactions, high temperature and high pressure synthesis reactions, and hydrogenation reactions. At present, high pressure catalytic hydrogenation reactions have high requirements for hydrogenation reactors. It is not easy for the catalyst to fully contact with the reactants when added to the hydrogenation reactor, and the catalytic reaction efficiency is low. In addition, the catalyst needs to be uniformly recovered before it can be used again. Utility Model Content
[0004] In view of the above deficiencies in the prior art, the technical problem to be solved by the utility model is to provide a neopentyl glycol production device to increase the contact area between the catalyst and the reactants, promote the catalytic reaction, and increase the service life of the catalyst.
[0005] The technical solution adopted by the utility model to solve its technical problems is:
[0006] The neopentyl glycol production device described in the utility model comprises a reactor 1 and a reactor 2, wherein the bottom of the reactor 1 is connected with the top of the reactor 2, a high-pressure mixing chamber is arranged on the top of the reactor 1, a first catalyst bed layer and a second catalyst bed layer are arranged inside the reactor 1 from top to bottom, the reactor 1 is connected with a heat exchanger, a liquid distributor, a catalyst fixed bed layer 1, a catalyst fixed bed layer 2 and a catalyst fixed bed layer 3 are arranged inside the reactor 2 from top to bottom, a jacket 1, a jacket 2 and a jacket 3 are arranged on the outside of the catalyst fixed bed layer 1, the catalyst fixed bed layer 2 and the catalyst fixed bed layer 3 respectively; the top of the reactor 1 is respectively connected with a raw material pipeline and a hydrogen pipeline, the bottom of the reactor 2 is connected with a gas-liquid separation tank, and the gas-liquid separation tank is connected with a product storage tank.
[0007] in:
[0008] The lower part of the heat exchanger is provided with a hot water inlet, and the upper part of the heat exchanger is provided with a hot water outlet.
[0009] The bottom of the reactor is connected to the inlet of the heat exchanger, and the outlet of the heat exchanger is connected to the raw material pipeline.
[0010] A material pump is arranged on the pipeline connected to the bottom of the reactor and the inlet of the heat exchanger.
[0011] A material pump is arranged on the pipeline between the reactor 1 and the reactor 2.
[0012] The liquid distributor is provided with a plurality of through holes.
[0013] The bottoms of the jackets 1, 2 and 3 are respectively provided with cooling water inlets, and the tops of the jackets 1, 2 and 3 are respectively provided with cooling water outlets.
[0014] A material pump is arranged on the pipeline between the second reactor and the gas-liquid separation tank.
[0015] A tail gas pipeline is arranged on the top of the gas-liquid separation tank.
[0016] A material pump is arranged on the pipeline between the gas-liquid separation tank and the product storage tank.
[0017] The beneficial effects of the utility model are:
[0018] The utility model can fix the catalyst so that the catalyst can fully contact with the reactant, thereby increasing the reaction efficiency, increasing the service life of the catalyst, and reducing the operation of separating the catalyst and the reaction product.
[0019] While the reaction liquid in the reactor one is circulated and cooled through the heat exchanger to dissipate heat, hydrogen is introduced for mixing so that the reaction liquid and hydrogen can fully react. After the reaction, the hydrogen and the reaction liquid are sent to the reactor two. The catalyst fixed bed layer one, the catalyst fixed bed layer two and the catalyst fixed bed layer three can ensure that the catalyst can fully play its role and improve the reaction efficiency. The setting of the jacket one, the jacket two and the jacket three can help control the reaction temperature and ensure that the temperature of each layer of catalyst can be individually regulated, thereby optimizing the reaction conditions and increasing the conversion rate of hydroxypivalaldehyde to more than 99%. BRIEF DESCRIPTION OF THE DRAWINGS
[0020] Figure 1 It is a schematic diagram of the structure of the utility model;
[0021] In the figure: 1. Reactor 1; 2. Reactor 2; 3. Gas-liquid separation tank; 4. Raw material pipeline; 5. Hydrogen pipeline; 6. Heat exchanger; 7. Product storage tank; 8. Tail gas pipeline; 101. High-pressure mixing chamber; 102. First catalyst bed; 103. Second catalyst bed; 201. Liquid distributor; 202. Catalyst fixed bed 1; 203. Catalyst fixed bed 2; 204. Catalyst fixed bed 3; 205. Jacket 1; 206. Jacket 2; 207. Jacket 3. DETAILED DESCRIPTION
[0022] The embodiments of the present utility model are further described below in conjunction with the accompanying drawings.
[0023] Example 1
[0024] like Figure 1 As shown, the neopentyl glycol production device described in the utility model includes a reactor 1 and a reactor 2, the bottom of the reactor 1 is connected to the top of the reactor 2, a high-pressure mixing chamber 101 is arranged on the top of the reactor 1, a first catalyst bed 102 and a second catalyst bed 103 are arranged from top to bottom in the reactor 1, the reactor 1 is connected to a heat exchanger 6, a liquid distributor 201, a catalyst fixed bed 1 202, a catalyst fixed bed 2 203 and a catalyst fixed bed 3 204 are arranged from top to bottom in the reactor 2, and a jacket 1 205, a jacket 2 206 and a jacket 3 207 are respectively arranged on the outside of the catalyst fixed bed 1 202, the catalyst fixed bed 2 203 and the catalyst fixed bed 3 204; the top of the reactor 1 is respectively connected to a raw material pipeline 4 and a hydrogen pipeline 5, the bottom of the reactor 2 is connected to a gas-liquid separation tank 3, and the gas-liquid separation tank 3 is connected to a product storage tank 7.
[0025] The high-pressure mixing chamber 101 can fully mix hydroxypivalaldehyde and hydrogen to facilitate the catalytic reaction. The layered fixing of the catalyst can make the reaction liquid fully contact with the catalyst when flowing through the first catalyst bed 102, the second catalyst bed 103, the catalyst fixed bed 1 202, the catalyst fixed bed 203 and the catalyst fixed bed 3 204, thereby improving the reaction efficiency.
[0026] A hot water inlet is provided at the lower portion of the heat exchanger 6 , and a hot water outlet is provided at the upper portion of the heat exchanger 6 .
[0027] The bottom of the reactor 1 is connected to the inlet of the heat exchanger 6, and the outlet of the heat exchanger 6 is connected to the raw material pipeline 4. The heat exchanger 6 can regulate the temperature of the reaction liquid inside the reactor 1 to ensure the stability of the reaction temperature.
[0028] A material pump is provided on the pipeline connecting the bottom of the reactor 1 and the inlet of the heat exchanger 6.
[0029] A material pump is provided on the pipeline between reactor 1 and reactor 2.
[0030] The liquid distributor 201 is provided with a plurality of through holes. The through holes on the liquid distributor 201 can evenly distribute the reaction liquid and hydrogen onto the catalyst fixed bed layer 1 202 .
[0031] The bottom of jacket 1 205, jacket 2 206 and jacket 3 207 are respectively provided with cooling water inlets, and the tops of jacket 1 205, jacket 2 206 and jacket 3 207 are respectively provided with cooling water outlets. Jacket 1 205, jacket 2 206 and jacket 3 207 can respectively regulate the temperature in catalyst fixed bed 1 202, catalyst fixed bed 2 203 and catalyst fixed bed 3 204 to ensure the stability of the catalytic reaction in reactor 2 2.
[0032] A material pump is provided on the pipeline between the reactor 2 2 and the gas-liquid separation tank 3 .
[0033] A tail gas pipeline 8 is provided on the top of the gas-liquid separation tank 3. A decompression operation is performed in the gas-liquid separation tank 3 to separate the gas and the neopentyl glycol product.
[0034] A material pump is provided on the pipeline between the gas-liquid separation tank 3 and the product storage tank 7 .
[0035] Working principle and process:
[0036] Hydroxypivalaldehyde and hydrogen are added to the top of the reactor-1 through the raw material pipeline 4 and the hydrogen pipeline 5 respectively, and the hydrogen and hydroxypivalaldehyde enter the high-pressure mixing chamber 101 for full mixing, and the mixed gas-liquid two phases pass through the first catalyst bed 102 and the second catalyst bed 103 in turn for catalytic hydrogenation reaction under the conditions of temperature of 95-110°C and pressure of 4.0MPa, and the reaction liquid after the reaction enters the heat exchanger 6 from the bottom of the reactor-1 for heat exchange, and after heat exchange, it re-enters the reactor-1 and introduces hydrogen for full reaction, and the reaction liquid and hydrogen in the reactor-1 are The reaction liquid is transported to reactor two 2 for reaction, and the reaction liquid is distributed by a liquid distributor 201. Under the conditions of a temperature of 97-110°C and a pressure of 4.0 MPa, the reaction liquid and hydrogen pass through catalyst fixed bed one 202, catalyst fixed bed two 203 and catalyst fixed bed three 204 in sequence to continue the reaction. After the reaction is completed, the reaction products in reactor two 2 are uniformly transported to a gas-liquid separation tank 3 for decompression separation to obtain a neopentyl glycol product and tail gas. The tail gas is recovered through an tail gas pipeline 8, and the neopentyl glycol product is transported to a product storage tank 7 for storage.
Claims
1. A neopentyl glycol production device, comprising a reactor 1 (1) and a reactor 2 (2), wherein the bottom of the reactor 1 (1) is connected to the top of the reactor 2 (2), characterized in that: A high-pressure mixing chamber (101) is arranged at the top of the reactor 1 (1); a first catalyst bed (102) and a second catalyst bed (103) are arranged inside the reactor 1 (1) from top to bottom; the reactor 1 (1) is connected to a heat exchanger (6); a liquid distributor (201), a catalyst fixed bed 1 (202), a catalyst fixed bed 2 (203) and a catalyst fixed bed 3 (204) are arranged inside the reactor 2 (2) from top to bottom; a jacket 1 (205), a jacket 2 (206) and a jacket 3 (207) are arranged outside the catalyst fixed bed 1 (202), the catalyst fixed bed 2 (203) and the catalyst fixed bed 3 (204); the top of the reactor 1 (1) is connected to a raw material pipeline (4) and a hydrogen pipeline (5); the bottom of the reactor 2 (2) is connected to a gas-liquid separation tank (3); and the gas-liquid separation tank (3) is connected to a product storage tank (7).
2. The neopentyl glycol production device according to claim 1, characterized in that: A hot water inlet is provided at the lower portion of the heat exchanger (6), and a hot water outlet is provided at the upper portion of the heat exchanger (6).
3. The neopentyl glycol production device according to claim 1, characterized in that: The bottom of the reactor 1 (1) is connected to the inlet of the heat exchanger (6), and the outlet of the heat exchanger (6) is connected to the raw material pipeline (4).
4. The neopentyl glycol production device according to claim 3, characterized in that: A material pump is provided on the pipeline connecting the bottom of the reactor 1 (1) and the inlet of the heat exchanger (6).
5. The neopentyl glycol production device according to claim 1, characterized in that: A material pump is provided on the pipeline between the reactor 1 (1) and the reactor 2 (2).
6. The neopentyl glycol production device according to claim 1, characterized in that: The liquid distributor (201) is provided with a plurality of through holes.
7. The neopentyl glycol production device according to claim 1, characterized in that: The bottoms of jacket 1 (205), jacket 2 (206) and jacket 3 (207) are respectively provided with cooling water inlets, and the tops of jacket 1 (205), jacket 2 (206) and jacket 3 (207) are respectively provided with cooling water outlets.
8. The neopentyl glycol production device according to claim 1, characterized in that: A material pump is provided on the pipeline between the second reactor (2) and the gas-liquid separation tank (3).
9. The neopentyl glycol production device according to claim 1, characterized in that: An exhaust gas pipeline (8) is arranged on the top of the gas-liquid separation tank (3).
10. The neopentyl glycol production device according to claim 1, characterized in that: A material pump is provided on the pipeline between the gas-liquid separation tank (3) and the product storage tank (7).