Catalytic hydrogenation comprehensive treatment system for butanol and octanol
By modifying the butoctanol catalytic hydrogenation reactor, and setting up multiple columns and related pipelines with a fan-shaped radial cross-section, the problems of hot spots and fly temperature in the existing process are solved, and more stable reaction operations and greater load adaptability are achieved.
Patent Information
- Application Number
- CN202420732141.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-10
- Publication Date
- 2025-03-18
- Estimated Expiration
- 2034-04-10
AI Technical Summary
In the existing butoctanol catalytic hydrogenation process, hot spots and flying temperatures are prone to occur, resulting in reduced reaction selectivity, deterioration of catalysts, and limited adjustment time.
By transforming the butoctanol catalytic hydrogenation reactor, the inside of the tank is divided into several columns with a fan-shaped radial cross-section. Each column is equipped with a hydrogenation reaction tube group, a catalyst backup tube group and a thermocouple tube, and an aldehyde branch tube, a backup pipeline, a gas distribution tube and a valve, providing a means to quickly deal with hot spots and fly temperature phenomena.
It effectively prevents the occurrence of hot spots and fly temperature phenomena, provides a quick means to control fly temperature, and improves the operating elasticity and load adaptability of the device.
Smart Images
Figure CN222624489U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of catalytic hydrogenation of butanol and octanol, and more specifically to a system for comprehensive treatment of catalytic hydrogenation of butanol and octanol. Background Art
[0002] Catalytic hydrogenation of butanol and octanol is an important part of the butanol production process, and is used for the hydrogenation of butyraldehyde and octenal. Taking butyraldehyde as an example, butyraldehyde from the butyraldehyde gas phase hydrogenation evaporator enters the butyraldehyde converter after being overheated in the butyraldehyde converter feed heater, and is hydrogenated in the converter to form crude mixed butanol. The converter is a shell and tube fixed bed reactor. The reactants flow upward and undergo hydrogenation through a vertical tube pass containing a hydrogenation catalyst. The hydrogenation reaction is an exothermic reaction; the heat generated heats the condensed water fed into the reactor shell into low-pressure steam. The butyraldehyde gas phase hydrogenation ejector is used to increase the pressure of the low-pressure steam and enter the corresponding steam main pipe for gas supply.
[0003] The butyl octanol hydrogenation process has achieved a transition from copper-nickel catalyst to copper-zinc catalyst, and copper-zinc catalyst is the main catalyst at this stage. Taking VAH catalyst as an example, its physical properties are shown in Table 1.
[0004] Table 1
[0005]
[0006] Generally speaking, there are two factors that determine the reaction rate of aldehyde hydrogenation, one is the reaction equilibrium constant, and the other is the chemical reaction rate. The reaction equilibrium constant of aldehyde hydrogenation itself is extremely large and can be regarded as an irreversible reaction, so this factor can be temporarily ignored. The chemical reaction rate is positively correlated with the temperature of the reactants, and the reaction itself is a highly exothermic reaction. This means that if the reaction is not controlled, within a certain range, the reaction temperature will rise rapidly and faster and faster. Therefore, the reactor uses a tube bundle to load the catalyst, increase the heat exchange area, and remove the heat in time to achieve the process purpose.
[0007] The catalyst temperature distribution generally has a highest point, called a "hot spot". Before the hot spot, the heat release rate is greater than the heat transfer rate, and the bed temperature rises. After the hot spot, the opposite is true, so the bed temperature gradually decreases. Controlling the hot spot temperature is the key to a smooth reaction. If the hot spot temperature is too high, the reaction selectivity will be reduced, the catalyst will deteriorate, and even the reaction will lose stability, resulting in a temperature runaway phenomenon. Temperature runaway is also commonly known as reactor temperature runaway, which refers to the phenomenon that when the reactor is in an unstable operating state, when there is a small disturbance in the operating parameters or reaction conditions, the temperature of a part of the reactor or the entire reactor will rise sharply.
[0008] As for the hydrogenation reaction of butyl octanol, whether it is butyraldehyde or octenal, the reaction itself is a strong exothermic reaction with a large equilibrium constant, which can be regarded as an irreversible reaction. Therefore, the most obvious influence on the reaction rate is the reaction temperature, and the two are positively correlated. Therefore, once there is a load change or misoperation, it is easy to cause a temperature runaway phenomenon, and the adjustment time is extremely limited. Utility Model Content
[0009] The purpose of the utility model is to overcome the deficiencies in the prior art and propose a system for comprehensive treatment of catalytic hydrogenation of butyl octanol. The utility model prevents the occurrence of temperature runaway phenomenon from the root, eliminates hot spots, provides control means for controlling temperature runaway phenomenon, increases the maximum load of the equipment, and improves the flexibility of reaction operation by modifying the catalytic hydrogenation reactor of butyl octanol.
[0010] The purpose of the utility model is achieved through the following technical solutions.
[0011] The utility model discloses a system for comprehensive treatment of catalytic hydrogenation of butanol and octanol, comprising a catalytic hydrogenation reactor of butanol and octanol, wherein the catalytic hydrogenation reactor of butanol and octanol comprises an outlet head, a tank body and an inlet head connected in sequence from top to bottom, wherein the outlet head and the inlet head of the catalytic hydrogenation reactor of butanol and octanol are respectively connected with an outlet main pipe and an aldehyde inlet main pipe, wherein an outlet grid plate and an inlet grid plate are respectively arranged at the upper and lower ends of the tank body of the butanol and octanol catalytic hydrogenation reactor, an outlet tube sheet and an inlet tube sheet are respectively arranged at the bottom of the outlet grid plate and the top of the inlet grid plate, wherein the inside of the tank body of the butanol and octanol catalytic hydrogenation reactor is equally divided into a plurality of columns with fan-shaped radial cross sections, wherein a hydrogenation reaction tube group, a catalyst spare tube group and a thermocouple tube for monitoring hot spot positions are arranged in each column;
[0012] The gas outlet of the hydrogenation reaction tube group in each column is connected to the gas outlet main pipe, and the gas inlet of the hydrogenation reaction tube group in each column is connected to the aldehyde gas inlet main pipe through the aldehyde branch pipe. Each aldehyde branch pipe is sequentially provided with an aldehyde branch pipe main valve and a reaction tube control valve along the gas flow direction, and each aldehyde branch pipe is connected to a hydrogen source and a nitrogen source;
[0013] A check valve is provided at the outlet of the catalyst spare pipe group in each column, and the outlet of the catalyst spare pipe group in each column is connected to the main outlet pipe. The air inlet of the catalyst spare pipe group in each column is connected to the gas distribution pipe located in the air inlet head, and each gas distribution pipe is connected to the outlet of the aldehyde branch pipe main valve on the corresponding aldehyde branch pipe through a spare pipeline, and each spare pipeline is provided with a spare pipe control valve.
[0014] Furthermore, the air inlet and the air outlet of the hydrogenation reaction tube group in each column of the butyl octanol catalytic hydrogenation reactor are fixedly connected to the air inlet tube sheet and the air outlet tube sheet respectively.
[0015] Furthermore, the air inlet and air outlet of the catalyst standby tube group in each column of the butyl octanol catalytic hydrogenation reactor are fixedly connected to the air inlet tube sheet and the air outlet tube sheet respectively, and the air inlet of the catalyst standby tube group is connected to a gas split pipe located at the lower end of the air inlet grid plate.
[0016] Furthermore, the temperature measurement points of the thermocouple tube in each column are distributed identically and evenly in the axial and radial directions, and the thermocouple tube in each column is fixedly connected to the air inlet tube sheet.
[0017] Furthermore, the hydrogen source and the nitrogen source are both connected to the aldehyde branch pipe part of the air inlet of each aldehyde branch pipe main valve.
[0018] Furthermore, all aldehyde branch pipe main valves, spare pipe control valves, and reaction pipe control valves are arranged outside the butyl octanol catalytic hydrogenation reactor.
[0019] Compared with the prior art, the beneficial effects brought about by the technical solution of the utility model are:
[0020] The tank part of the butyl octanol catalytic hydrogenation reactor in the utility model is equally divided into a number of columns with fan-shaped radial cross-sections, each column is provided with a hydrogenation reaction tube group, a catalyst spare tube group and a thermocouple tube for monitoring the hot spot position, each column corresponds to a group of aldehyde branch pipes, spare pipelines, gas distribution pipes and valves, which provide a means of rapid processing for processing hot spots and temperature runaway phenomena, increase the operational flexibility of the process flow itself, and provide more space for product adjustment. The utility model achieves the goal of maintaining the butyl octanol catalytic hydrogenation capacity load while reducing the possibility of hot spots and temperature runaway by improving the butyl octanol catalytic hydrogenation reactor. BRIEF DESCRIPTION OF THE DRAWINGS
[0021] Figure 1 This is a schematic diagram of the system for comprehensive treatment of butyl octanol catalytic hydrogenation according to the utility model.
[0022] Figure markings: 1-aldehyde inlet main pipe, 2-aldehyde branch pipe main valve, 3-spare pipe control valve, 4-nitrogen source, 5-reaction tube control valve, 6-gas distribution pipe, 7-air inlet grid plate, 8-thermocouple tube, 9-catalyst spare pipe group, 10-hydrogenation reaction tube group, 11-check valve, 12-air outlet grid plate, 13-air outlet main pipe, 14-hydrogen source, 15-butyl octanol catalytic hydrogenation reactor, 1501-air outlet head, 1502-tank body, 1503-air inlet head, 16-aldehyde branch pipe, 17-air outlet tube sheet, 18-air inlet tube sheet, 19-spare pipeline. DETAILED DESCRIPTION
[0023] The utility model is further described below in conjunction with the accompanying drawings.
[0024] like Figure 1 As shown, the system for comprehensive treatment of butyl octanol catalytic hydrogenation of the utility model comprises a butyl octanol catalytic hydrogenation reactor 15, the general structure of which is similar to that of a floating head heat exchanger, and mainly comprises an outlet head 1501, a tank body 1502, and an inlet head 1503 connected in sequence from top to bottom. The outlet head 1501 is connected to the outlet main pipe 13. The upper and lower ends of the tank body 1502 are respectively provided with an outlet grid plate 12 and an inlet grid plate 7, and the bottom of the outlet grid plate 12 and the top of the inlet grid plate 7 are respectively provided with an outlet tube sheet 17 and an inlet tube sheet 18.
[0025] The interior of the tank body 1502 is equally divided into several cylinders with fan-shaped radial cross sections. Preferably, the interior of the tank body 1502 can be equally divided into six cylinders with fan-shaped radial cross sections, each of which can be based on the radial section of the bottom of the tank body 1502 as the bottom, and the axial length of the tank body 1502 (the height of the remaining cylinder of the gas outlet head 1501 and the gas inlet head 1503 is removed from the gas outlet tube sheet 17 and the gas inlet tube sheet 18) as the height. A hydrogenation reaction tube group 10, a catalyst standby tube group 9, and a thermocouple tube 8 for monitoring the hot spot position are arranged in each column. The catalyst standby tube group 9 has the same specifications as the hydrogenation reaction tube group 10.
[0026] The air inlet and air outlet of the hydrogenation reaction tube group 10 in each column are fixedly connected to the air inlet tube sheet 18 and the air outlet tube sheet 17 respectively. The air outlet of the hydrogenation reaction tube group 10 in each column is connected to the air outlet main pipe 13, and the air inlet of the hydrogenation reaction tube group 10 in each column is connected to the aldehyde air inlet main pipe 1 through an aldehyde branch pipe 16, and other aldehydes such as butyraldehyde or octenaldehyde are introduced into the aldehyde air inlet main pipe 1. Each aldehyde branch pipe 16 is sequentially provided with an aldehyde branch pipe main valve 2 and a reaction tube control valve 5 along the gas flow direction, and each aldehyde branch pipe 16 is connected to a hydrogen source 14 and a nitrogen source 4. Wherein, the hydrogen source 14 and the nitrogen source 4 can be connected to the aldehyde branch pipe 16 part of the air inlet of each aldehyde branch pipe main valve 2.
[0027] The air inlet and air outlet of the catalyst standby pipe group 9 in each column are fixedly connected to the air inlet tube sheet 18 and the air outlet tube sheet 17 respectively. The air outlet of the catalyst standby pipe group 9 in each column is connected to the air outlet main pipe 13, and the air outlet of the catalyst standby pipe group 9 in each column is provided with a check valve 11 to prevent the butyl octanol catalytic hydrogenation reactor 15 from backflowing into the catalyst standby pipe group 9. The air inlet of the catalyst standby pipe group 9 in each column is connected to a gas distribution pipe 6 located in the air inlet head 1503, and each gas distribution pipe 6 is connected to the air outlet of the aldehyde branch pipe main valve 2 on the aldehyde branch pipe 16 corresponding to the column through a standby pipeline 19, and each standby pipeline 19 is provided with a standby pipe control valve 3. Among them, one main body corresponds to one gas split pipe 6, and the gas split pipes 6 are all located at the lower end of the air inlet grid plate 7.
[0028] The thermocouple tubes 8 in each column are fixedly connected to the air inlet tube sheet 18, and the temperature measurement points of the thermocouple tubes 8 in each column are distributed in the same and uniform manner in the axial and radial directions. For example, all the thermocouple tubes 8 provide a total of 60 temperature measurement points, which are divided into 6 groups distributed at equal intervals along the axial direction of the tank body 1502, each group of 10 and 10 temperature measurement points are located on the same radial section of the tank body 1502, and the 10 temperature measurement points are evenly distributed on the radial section where they are located, and the 6 radial sections divide the tank body 1502 cylinder into six equal parts (for six equal parts, it is better to implement 50 temperature measurement points, which are evenly distributed).
[0029] Preferably, in the above-mentioned system for comprehensive treatment of butyl octanol catalytic hydrogenation, all aldehyde branch pipe main valves 2, spare pipe control valves 3, and reaction pipe control valves 5 are arranged outside the butyl octanol catalytic hydrogenation reactor 15 to prevent excessive temperature from affecting the life of each control valve. The air inlet tube sheet 18 is provided with a plurality of tube-side air inlets that are connected to the air inlets of all hydrogenation reaction tube groups 10 and catalyst spare tube groups 9 in a one-to-one correspondence; all air outlet tube sheets 17 are provided with a plurality of tube-side air outlets that are connected to the air outlets of all hydrogenation reaction tube groups 10 and catalyst spare tube groups 9 in a one-to-one correspondence. The connection points of all aldehyde branch pipes 16 and the distribution of the aldehyde branch pipe main valves 2 and reaction pipe control valves 5 thereon are the same, and the connection points of all spare pipelines 19 and the distribution of the spare pipe control valves 3 and gas distribution pipes 6 thereon are the same. The axes of all catalyst spare tube groups 9 and hydrogenation reaction tube groups 10 in the butyl octanol catalytic hydrogenation reactor 15 are parallel to the axis of the tank body 1502. The radial sections of the catalyst spare tube group 9 can be evenly distributed on the radial section of the tank body 1502 , without affecting the internal heat exchange process of the butyl octanol catalytic hydrogenation reactor 15 .
[0030] The working principle of the utility model of the system for comprehensive treatment of butyl octanol catalytic hydrogenation:
[0031] The hot spot is detected in the butyl octanol catalytic hydrogenation reactor 15 by the thermocouple tube 8. When the temperature runaway phenomenon occurs, the hot spot position is observed and recorded. According to the hot spot position, the spare pipe control valve 3 corresponding to the column where the hot spot position is located is opened, and the catalyst spare pipe group 9 corresponding to the hot spot position is opened, so as to timely shunt the butyraldehyde gas load in the hydrogenation reaction tube group 10 and achieve rapid cooling. The opening of the spare pipe control valve 3 and the corresponding reaction tube control valve 5 are adjusted, and the temperature change in the butyl octanol catalytic hydrogenation reactor 15 is observed and controlled until the hot spot disappears and the temperature runaway phenomenon is controlled.
[0032] When inspecting and replacing the catalyst in the hydrogenation reaction tube group 10, the specific location of the hot spot temperature runaway and the corresponding hydrogenation reaction tube group 10 are marked according to the hot spot and the temperature runaway phenomenon records. When the catalyst is loaded, the hydrogenation reaction tube group 10 in normal operation is loaded with fresh catalyst. The hydrogenation reaction tube group 10 with hot spot temperature runaway is loaded using catalyst grading technology, and the hot spot position is loaded with a mixture of aged catalyst and fresh catalyst. Specifically, the hot spot position is centered, and the pipe section with a length of 0.8m is filled with fresh catalyst and aged catalyst mixed with grading, and the aged catalyst content is 20-80%, and the rest is still filled with fresh catalyst. After all the hydrogenation reaction tube groups 10 are loaded, all tubes are in a state of being filled with catalysts. Here, fresh catalyst refers to unused catalyst, aged catalyst refers to used catalyst, and fresh catalyst and aged catalyst use the same catalyst. In addition, the catalyst type in the catalyst spare tube group 9 is the same as the catalyst type in the hydrogenation reaction tube group 10, and the loading method and principle are also the same. The catalyst spare tube group 9 gives priority to fresh catalyst.
[0033] After all the tube groups of the butyl octanol catalytic hydrogenation reactor 15 are replaced with nitrogen, the catalyst is hydrogenated and activated; the catalyst in the hydrogenation reaction tube group 10 is put into normal use after hydrogenation and activation, and the catalyst standby tube group 9 is sealed at both ends of the standby tube control valve 3 and the check valve 11 to enter the standby state for use at any time.
[0034] The utility model of the present invention prevents the generation of hot spots and temperature runaway phenomena in the catalytic hydrogenation reaction device of butanol and octanol from the root, provides a fast and effective means for controlling the temperature runaway phenomenon, and at the same time improves the operational flexibility of the device, so that the process can adapt to more drastic load changes.
[0035] Although the functions and working processes of the utility model are described above in conjunction with the accompanying drawings, the utility model is not limited to the above-mentioned specific functions and working processes, and the above-mentioned specific implementation methods are merely illustrative rather than restrictive. Under the enlightenment of the utility model, ordinary technicians in this field can also make many forms without departing from the scope of protection of the purpose of the utility model and the claims, which are all within the protection of the utility model.
Claims
1. A system for catalytic hydrogenation of 1,2-butanol and octanols, comprising a catalytic hydrogenation reactor (15), wherein the catalytic hydrogenation reactor (15) comprises an outlet head (1501), a tank body (1502), and an air inlet head (1503) connected in sequence from top to bottom, wherein the outlet head (1501) and the air inlet head (1503) of the catalytic hydrogenation reactor (15) are respectively connected to an outlet main pipe (13) and an aldehyde inlet main pipe (1), wherein the tank body (1502) of the catalytic hydrogenation reactor (15) is provided with an outlet grid plate (12) and an air inlet grid plate (7) at the upper and lower ends thereof, respectively, and an outlet tube sheet (17) and an air inlet tube sheet (18) are respectively provided at the bottom of the outlet grid plate (12) and the top of the air inlet grid plate (7), wherein: The interior of the tank body (1502) of the butyl octanol catalytic hydrogenation reactor (15) is equally divided into a number of columns with fan-shaped radial cross-sections, each of which is provided with a hydrogenation reaction tube group (10), a catalyst spare tube group (9) and a thermocouple tube (8) for monitoring the hot spot position; The gas outlet of the hydrogenation reaction tube group (10) in each column is connected to the gas outlet main pipe (13), and the gas inlet of the hydrogenation reaction tube group (10) in each column is connected to the aldehyde gas inlet main pipe (1) through the aldehyde branch pipe (16). Each aldehyde branch pipe (16) is sequentially provided with an aldehyde branch pipe main valve (2) and a reaction tube control valve (5) along the gas flow direction, and each aldehyde branch pipe (16) is connected to a hydrogen source (14) and a nitrogen source (4); The gas outlet of the catalyst standby pipe group (9) in each column is provided with a check valve (11), the gas outlet of the catalyst standby pipe group (9) in each column is connected to the gas outlet main pipe (13), the gas inlet of the catalyst standby pipe group (9) in each column is connected to the gas distribution pipe (6) located in the gas inlet head (1503), each gas distribution pipe (6) is connected to the gas outlet of the aldehyde branch pipe main valve (2) on the corresponding aldehyde branch pipe (16) through a standby pipeline (19), and each standby pipeline (19) is provided with a standby pipe control valve (3).
2. The system for comprehensive treatment of butyl octanol catalytic hydrogenation according to claim 1, characterized in that: The air inlet and the air outlet of the hydrogenation reaction tube group (10) in each column of the butyl octanol catalytic hydrogenation reactor (15) are fixedly connected to the air inlet tube sheet (18) and the air outlet tube sheet (17) respectively.
3. The system for comprehensive treatment of butyl octanol catalytic hydrogenation according to claim 1, characterized in that: The air inlet and air outlet of the catalyst standby tube group (9) in each column of the butyl octanol catalytic hydrogenation reactor (15) are fixedly connected to the air inlet tube plate (18) and the air outlet tube plate (17) respectively, and the air inlet of the catalyst standby tube group (9) is connected to the gas distribution pipe (6) located at the lower end of the air inlet grid plate (7).
4. The system for comprehensive treatment of butyl octanol catalytic hydrogenation according to claim 1, characterized in that: The temperature measurement points of the thermocouple tube (8) in each column are distributed identically and evenly in the axial and radial directions, and the thermocouple tube (8) in each column is fixedly connected to the air inlet tube plate (18).
5. The system for comprehensive treatment of butyl octanol catalytic hydrogenation according to claim 1, characterized in that: The hydrogen source (14) and the nitrogen source (4) are both connected to the aldehyde branch pipe (16) portion of the gas inlet of each aldehyde branch pipe main valve (2).
6. The system for comprehensive treatment of butyl octanol catalytic hydrogenation according to claim 1, characterized in that: All aldehyde branch pipe main valves (2), spare pipe control valves (3) and reaction pipe control valves (5) are arranged outside the butyl octanol catalytic hydrogenation reactor (15).