Switchable catalyst double fixed bed reactor
By designing a switchable catalyst dual fixed bed reactor, the flexible switching of the reactor is achieved by using the settings of pipelines and switch valves, the problem of difficulty in adjusting the chemical synthesis route of fixed bed reactors in the prior art is solved, and the reaction efficiency and catalyst utilization efficiency are improved.
Patent Information
- Application Number
- CN202422145640.3
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-09-02
- Publication Date
- 2025-06-24
- Estimated Expiration
- 2034-09-02
AI Technical Summary
The existing fixed-bed reactors are difficult to adjust the chemical synthesis route, and can only perform one step of catalysis, resulting in the need to replace the device when the catalytic efficiency is reduced or the production target product changes, which wastes costs and time.
A switchable catalyst dual fixed bed reactor is designed. By reasonably setting up pipelines and switch valves, the first reactor and the second reactor can be switched in series or parallel, and can meet different production requirements.
It realizes that the chemical synthesis route can be adjusted without adding or replacing the equipment on the original equipment, reduces the workshop dismantling time and equipment cost, and improves the efficiency of catalyst utilization and reaction efficiency.
Smart Images
Figure CN223010505U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of catalytic devices, in particular to a switchable catalyst double fixed-bed reactor. Background Art
[0002] Disclosing the information of this background art section is only intended to enhance the overall understanding of the present utility model, and it is not necessarily regarded as an admission or an implication in any form that this information constitutes the prior art already known to those of ordinary skill in the art.
[0003] At the present stage, the vast majority of dehydration reactions need to be carried out under the catalysis of a catalyst. Therefore, a catalyst needs to be loaded into a reactor for catalysis.
[0004] After the dehydration reaction catalyst is used for a long time, its activity will gradually decrease, resulting in a decline in the reaction efficiency. Therefore, it is necessary to regenerate the catalyst to remove the impurities and inactivated substances accumulated on the surface of the catalyst, restore the activity of the catalyst, and improve the reaction efficiency.
[0005] In some fixed-bed reactors, the dehydration reaction and the regeneration of the catalyst are often realized by switching the regeneration gas and the raw material gas. Even in a multi-fixed-bed reactor, only one-step catalysis is often carried out. When the catalytic energy efficiency of the reactor decreases, or the production target product or production process changes, at this time, two-step catalysis is required. The existing devices are difficult to adjust the chemical synthesis route of the device, and can only be discarded and replaced with new devices, which is not only time-consuming and laborious, but also enterprises need to configure multiple production lines, seriously wasting costs. Summary of the Utility Model
[0006] In order to solve the deficiencies of the prior art, the purpose of the present utility model is to provide a switchable catalyst double fixed-bed reactor, which solves the problem that the existing fixed-bed reactor is difficult to adjust and can only carry out one-step catalytic reactions.
[0007] In order to achieve the above purpose, the technical solution of the present utility model is as follows:
[0008] A switchable catalyst double fixed-bed reactor includes:
[0009] A first inlet pipe, a second inlet pipe, a first reactor, a second reactor, and a total product gas outlet pipe;
[0010] The front end of the first reactor is connected to the first inlet pipe through a switching valve three, the front end of the second reactor is connected to the second inlet pipe through a switching valve two, the first inlet pipe and the second inlet pipe are connected through a first branch pipe, the first branch pipe is arranged in front of the switching valve three and the switching valve two, and a switching valve one is arranged on the first branch pipe;
[0011] The first reactor and the second reactor are connected to the total product gas outlet pipe through the eighth branch pipe; the first reactor is connected to the eighth branch pipe through the eleventh branch pipe, and the second reactor is connected to the eighth branch pipe through the fourth branch pipe; a switching valve eight is provided on the eighth branch pipe, and a switching valve four is provided on the fourth branch pipe;
[0012] A ninth branch pipe is provided on the second inlet pipe between the switching valve two and the second reactor, the other end of the ninth branch pipe is connected to the total product gas outlet pipe, and a switching valve nine is provided on the ninth branch pipe.
[0013] In the utility model, the reactors are connected through reasonably arranged pipes, and switching valves are arranged at appropriate positions on the pipes. By controlling the opening and closing of different switching valves, different gas passages are obtained, and the separate use, series connection or parallel connection of the first reactor and the second reactor can be switched, so as to meet the requirements of different productions.
[0014] In some embodiments, the total product gas outlet pipe is further connected to a heat exchanger, and the heat exchanger is connected to a product storage tank.
[0015] In some embodiments, a heating device is further provided on the second reactor for heating the raw materials in the second reactor.
[0016] In some embodiments, the fourth branch pipe and the ninth branch pipe are further connected through a seventh branch pipe, one end of the seventh branch pipe is connected between the second reactor and the switching valve four, and the other end is connected between the switching valve nine and the total product gas outlet pipe.
[0017] In some embodiments, a sixth branch pipe is further provided on the seventh branch pipe, one end of the sixth branch pipe is a regenerated gas outlet, and a switching valve six is provided on the sixth branch pipe; a switching valve seven is further provided between the sixth branch pipe and the ninth branch pipe.
[0018] By adding the above-mentioned branch pipes and switching valves in the utility model, the regenerated gas enters through the inlet pipe, passes through the second reactor, regenerates the catalyst in the second reactor, and the waste gas is discharged through the regenerated gas outlet of the sixth branch pipe.
[0019] In some embodiments, a fifth branch pipe is further provided on the eleventh branch pipe, one end of the fifth branch pipe is connected between the fourth branch pipe and the switching valve eight, one end of the fifth branch pipe is a regenerated gas outlet, and a switching valve five is provided on the fifth branch pipe.
[0020] Through the above-mentioned settings of the branch pipes and switching valves, the regenerated gas enters through the inlet pipe, passes through the first reactor, regenerates the catalyst in the first reactor, and the waste gas is discharged through the regenerated gas outlet of the fifth branch pipe.
[0021] In some embodiments, the product storage tank and the heat exchanger are connected through a pipe, and a carrier gas outlet is provided on the pipe.
[0022] In some embodiments, the first intake pipe and the eighth branch pipe are connected through the tenth branch pipe. The tenth branch pipe is arranged between the switching valve three and the switching valve eight, and a switching valve ten is also arranged on the tenth branch pipe.
[0023] In some embodiments, solid catalysts are also fixed in the first reactor and the second reactor.
[0024] In some embodiments, a heating device is also arranged on the second reactor to heat the raw materials in the second reactor.
[0025] In some embodiments, both the branch pipes and the intake pipes are made of stainless steel.
[0026] The beneficial effects of the present utility model are as follows:
[0027] 1. Through the arrangement of the switching valves and pipelines, by controlling the opening and closing of different switching valves, different gas paths are obtained, and the separate use, series connection or parallel connection of the first reactor and the second reactor can be switched. Thus, the chemical synthesis route can be adjusted without adding, subtracting or replacing equipment on the original equipment, reducing the disassembly time and equipment cost of the workshop.
[0028] 2. Through the arrangement of the switching valves and pipelines, the separate dehydration and parallel dehydration of the first reactor and the second reactor can be realized, better controlling the reaction rate. It can also be used in series. After the raw material gas is dehydrated by the first reactor, it can then pass through the second reactor for continuous reaction to improve the reaction degree or carry out another reaction such as a heating reduction reaction. The chemical synthesis route can be adjusted without adding, subtracting or replacing equipment on the original equipment.
[0029] 3. Through the arrangement of the switching valves and pipelines, the catalyst regeneration of different reactors can be alternately carried out, enabling the device to continuously carry out the dehydration reaction. One of the two reactors is used for the dehydration reaction, and the other is used for the in-situ regeneration of the catalyst. The two reactors operate alternately, saving the time for catalyst replacement and regeneration. BRIEF DESCRIPTION OF THE DRAWINGS
[0030] The schematic diagram of the drawings forming a part of the present utility model is used to provide a further understanding of the present utility model. The schematic embodiments and descriptions thereof of the present utility model are used to explain the present utility model and do not constitute an improper limitation to the present utility model.
[0031] Figure 1 It is a schematic structural diagram of a switchable catalyst double fixed-bed reactor according to an embodiment of the present utility model.
[0032] Among them, 1 is the first inlet pipe; 2 is the second inlet pipe; 3 is the first reactor; 4 is the second reactor; 5 is the heat exchanger; 6 is the product storage tank; 7 is the on-off valve; 701 is the first on-off valve; 702 is the second on-off valve; 703 is the third on-off valve; 704 is the fourth on-off valve; 705 is the fifth on-off valve; 706 is the sixth on-off valve; 707 is the seventh on-off valve; 708 is the eighth on-off valve; 709 is the ninth on-off valve; 7010 is the tenth on-off valve; 8 is the branch pipe; 801 is the first branch pipe; 802 is the fourth branch pipe; 803 is the fifth branch pipe; 804 is the sixth branch pipe; 805 is the seventh branch pipe; 806 is the eighth branch pipe; 807 is the ninth branch pipe; 808 is the tenth branch pipe; 809 is the eleventh branch pipe; 9 is the total outlet pipe for the generated gas; 10 is the outlet for the carrier gas. Detailed implementation mode
[0033] Aiming at the problem that the existing fixed-bed reactor can only achieve one-step catalysis and it is difficult to adjust the chemical synthesis route, the present utility model proposes a switchable catalyst double fixed-bed reactor.
[0034] In order to enable those skilled in the art to more clearly understand the technical solution of the present utility model, the following will specifically describe the technical solution of the present utility model in detail with reference to specific embodiments.
[0035] The technical solution of the present utility model discloses a switchable catalyst double fixed-bed reactor, including: a first inlet pipe 1, a second inlet pipe 2, a first reactor 3, a second reactor 4, and a total outlet pipe 9 for the generated gas; the front end of the first reactor 3 is connected to the first inlet pipe 1 through the third on-off valve 703, the front end of the second reactor 4 is connected to the second inlet pipe 2 through the second on-off valve 702, the first inlet pipe 1 and the second inlet pipe 2 are connected through the first branch pipe 801, the first branch pipe 801 is arranged at the front end of the third on-off valve 703 and the second on-off valve 702, and a first on-off valve 701 is arranged on the first branch pipe 801; the first reactor 3 and the second reactor 4 are connected to the total outlet pipe 9 for the generated gas through the eighth branch pipe 806; the first reactor 3 is connected to the eighth branch pipe 806 through the eleventh branch pipe 809, and the second reactor 4 is connected to the eighth branch pipe 806 through the fourth branch pipe 802; an eighth on-off valve 708 is arranged on the eighth branch pipe 806, and a fourth on-off valve 704 is arranged on the fourth branch pipe 802; a ninth branch pipe 807 is arranged on the second inlet pipe 2 between the second on-off valve 702 and the second reactor 4, the other end of the ninth branch pipe 807 is connected to the total outlet pipe 9 for the generated gas, and a ninth on-off valve 709 is arranged on the ninth branch pipe 807. Through the above arrangement of pipelines and on-off valves, when in use, by controlling the opening and closing of different on-off valves, the separate use, series connection or parallel connection of the first reactor 3 and the second reactor 4 can be realized, so as to adjust the device to achieve one-step catalysis or two-step reaction.
[0036] Optionally, the total outlet pipe 9 of the generated gas is further connected to a heat exchanger 5, and the heat exchanger 5 is connected to a product storage tank 6. The product storage tank 6 and the heat exchanger 5 are connected by a pipeline, and a carrier gas outlet 10 is provided on the pipeline. When the raw material gas after the catalytic reaction passes through the heat exchanger 5, due to the different boiling points of different substances, the generated product condenses into a liquid in the heat exchanger 5 and flows through the pipeline to be temporarily stored in the product storage tank 6. The raw material gas that has not participated in the reaction passes through the pipeline and exits from the carrier gas outlet 10, and is collected or purified to meet the emission standards before being discharged.
[0037] Optionally, a heating device is further provided on the second reactor 4 for heating the raw materials in the second reactor 4. Specifically, the heating device preferably adopts an electric heater and is arranged on the surface of the second reactor 4 to heat the second reactor 4. When preparing 2-pyrrolidone using NHP, the first reactor 3 and the second reactor 4 are connected in series. NHP (1-hydroxy-2-piperidinecarboxylic acid) is catalytically dehydrated to form NVP (1-vinyl-2-pyrrolidone) under the action of a catalyst. The raw materials in the second reactor 4 are heated by the heating device, and NVP undergoes a reaction when heated in the second reactor 4 containing the catalyst, and is further heated to form 2-pyrrolidone. The catalyst in the second reactor 4 also further promotes the progress of the NHP dehydration reaction.
[0038] Optionally, the fourth branch pipe 802 and the ninth branch pipe 807 are further connected by a seventh branch pipe 805. One end of the seventh branch pipe 805 is connected between the second reactor 4 and the fourth switch valve 704, and the other end is connected between the ninth switch valve 709 and the total outlet pipe 9 of the generated gas. A sixth branch pipe 804 is further provided on the seventh branch pipe 805. One end of the sixth branch pipe 804 is a regenerated gas outlet, and a sixth switch valve 706 is provided on the sixth branch pipe 804; a seventh switch valve 707 is further provided between the sixth branch pipe 804 and the ninth branch pipe 807. When the catalytic performance of the catalyst in the reactor decreases, the regenerated gas enters the second reactor 4 through the inlet pipe to regenerate the catalyst in the second reactor 4. The waste gas passes through the fourth branch pipe 802 and the seventh branch pipe 805, and finally exits through the regenerated gas outlet of the sixth branch pipe 804.
[0039] Optionally, a fifth branch pipe 803 is further provided on the eleventh branch pipe 809. One end of the fifth branch pipe 803 is connected between the fourth branch pipe 802 and the eighth switch valve 708. One end of the fifth branch pipe 803 is a regenerated gas outlet, and a fifth switch valve 705 is provided on the fifth branch pipe 803. The regenerated gas passes through the inlet pipe to the first reactor 3 to regenerate the catalyst in the first reactor 3, and the waste gas passes through the eleventh branch pipe 809 and finally exits through the regenerated gas outlet of the fifth branch pipe 803.
[0040] Optionally, the first intake pipe 1 and the eighth branch pipe 806 are connected through the tenth branch pipe 808. The tenth branch pipe 808 is arranged between the third switching valve 703 and the eighth switching valve 708. A tenth switching valve 7010 is also arranged on the tenth branch pipe 808. The arrangement of the tenth branch pipe 808 enables the raw material gas to first complete the first-step reaction in the second reactor 4, enter the first reactor 3 through the fourth switching valve 704 to complete the second-step reaction, and the reacted gas enters the heat exchanger 5 through the tenth switching valve 7010. The ninth switching valve 709 is closed to prevent the reacted gas from re-entering the second reactor 4. A switching valve can be installed on the right side of the eighth branch pipe 806 to prevent the reacted gas from flowing back to the second reactor 4.
[0041] Optionally, solid catalysts are also fixed in the first reactor 3 and the second reactor 4 for catalytic reaction of the reactants.
[0042] Optionally, the branch pipes and the intake pipes are made of stainless steel, and the stainless steel is preferably 316L stainless steel.
[0043] The working principle of the present utility model is as follows:
[0044] 1. When it is necessary to alternately perform catalytic reaction and regeneration reduction in two reactors, open the third switching valve 703 of the first reactor 3 in the pipeline connected to the first intake gas path, close the other switching valves, so that the raw material gas enters the first reactor 3 for dehydration reaction. Open the eighth switching valve 708 at the lower end outlet of the first reactor 3, so that the reacted gas enters the heat exchanger 5, and the reacted gas is cooled to obtain a reaction solution, and then stored in the product storage tank 6. The carrier gas is discharged through the carrier gas outlet 10 to complete the dehydration reaction. Open the second switching valve 702 of the second reactor 4 connected to the second intake pipe 2, close the other switching valves, so that the gas required for in-situ regeneration of the catalyst enters the second reactor 4 for in-situ regeneration of the catalyst. Open the sixth switching valve 706 at the lower end of the second reactor 4, and discharge the regeneration gas through the regeneration gas outlet 5.
[0045] When the activity of the catalyst in the first reactor 3 decreases and the regeneration of the catalyst in the second reactor 4 is completed, similarly, by adjusting the second switching valve 702, the third switching valve 703, the fifth switching valve 705 and the seventh switching valve 707, the first reactor 3 can perform catalyst regeneration and the second reactor 4 can perform dehydration reaction.
[0046] 2. When dehydration reactions need to be carried out in two reactors simultaneously, open the first reactor 3 and the second reactor 4 switch valves three 703 and two 702 of the pipeline connected to the first inlet pipe 1, close the remaining switch valves, allow the raw material gas to enter the first reactor 3 and the second reactor 4 for dehydration reactions, open the switch valve eight 708 at the lower outlet of the first reactor 3, allow the reacted gas to enter the heat exchanger 5, complete the cooling of the gas to obtain the reaction liquid, and then store it in the product storage tank 6 to complete the dehydration reaction.
[0047] 3. When consecutive reactions need to be carried out in two reactors, open the first reactor 3 switch valve three 703 of the pipeline connected to the first inlet pipe 1, close the remaining switch valves, allow the raw material gas to enter the first reactor 3 for the first-step reaction, open the switch valve four 704 at the connection between the lower end of the first reactor 3 and the second reactor 4, allow the reacted gas to enter the second reactor 4 for the second-step reaction, open the switch valve nine 709 at the left end of the second reactor 4, allow the reaction gas to enter the heat exchanger 5, complete the cooling of the gas to obtain the reaction liquid, and then store it in the product storage tank 6 to complete the reaction.
[0048] Similarly, by adjusting the switch valves, the second reactor 4 can carry out the first-step reaction and the first reactor 3 can carry out the second-step reaction.
[0049] The device of the present utility model can, through the arrangement of pipelines and switch valves, carry out reactions with two reactors operating in parallel simultaneously; it can also achieve the alternate catalysis or regeneration of two catalysts for operation, saving the time for catalyst replacement and regeneration, such as being applied to dehydration reactions with most catalysts filled; it can also give full play to the energy efficiency of the catalyst when the energy efficiency of the catalyst decreases, connect the two reactors in series, and successively carry out the same reaction through the two reactors. If the production target product changes, the two reactors can also be connected in series to carry out a two-step reaction, with the first reactor carrying out the first-step intermediate reaction and the second reactor carrying out the second-step target product reaction, such as being applied to the preparation of 2-pyrrolidone: NHP (1-hydroxy-2-piperidinecarboxylic acid) is catalytically dehydrated to form NVP (1-vinyl-2-pyrrolidone), and further heating generates 2-pyrrolidone. If the production process changes and two kinds of materials are required, the two reactors can also be connected in series, with the first reactor serving as a preheating and material mixer and the second reactor serving as a reactor. The device of the present utility model has flexible operation and can be applied to a variety of chemical synthesis routes.
[0050] The above are only the preferred embodiments of the present utility model and are not used to limit the present utility model. For those skilled in the art, the present utility model can have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present utility model shall be included within the protection scope of the present utility model.
Claims
1. A switchable catalyst dual fixed bed reactor, characterized in that: include: A first air inlet pipe, a second air inlet pipe, a first reactor, a second reactor and a generated gas main outlet pipe; The front end of the first reactor is connected to the first air inlet pipe through the switch valve three, the front end of the second reactor is connected to the second air inlet pipe through the switch valve two, the first air inlet pipe and the second air inlet pipe are connected through the first branch pipe, the first branch pipe is arranged at the front ends of the switch valve three and the switch valve two, and the switch valve one is arranged on the first branch pipe; The first reactor and the second reactor are connected to the main outlet pipe of generated gas through the eighth branch pipe; the first reactor is connected to the eighth branch pipe through the eleventh branch pipe, and the second reactor is connected to the eighth branch pipe through the fourth branch pipe; a switch valve eight is arranged on the eighth branch pipe, and a switch valve four is arranged on the fourth branch pipe; a ninth branch pipe is arranged on the second air inlet pipe between the switch valve two and the second reactor, and the other end of the ninth branch pipe is connected to the main outlet pipe of generated gas, and a switch valve nine is arranged on the ninth branch pipe.
2. The switchable catalyst dual fixed bed reactor according to claim 1, characterized in that: The main outlet pipe of the generated gas is also connected to a heat exchanger, and the heat exchanger is connected to a product storage tank.
3. The switchable catalyst dual fixed bed reactor according to claim 1, characterized in that: The second reactor is also provided with a heating device for heating the raw materials in the second reactor.
4. The switchable catalyst dual fixed bed reactor according to claim 1, characterized in that: The fourth branch pipe and the ninth branch pipe are also connected through the seventh branch pipe, one end of the seventh branch pipe is connected between the second reactor and the switch valve four, and the other end is connected between the switch valve nine and the total outlet pipe of the generated gas.
5. The switchable catalyst dual fixed bed reactor according to claim 4, characterized in that: A sixth branch pipe is also arranged on the seventh branch pipe, one end of the sixth branch pipe is a regas outlet, and a switch valve six is arranged on the sixth branch pipe; a switch valve seven is also arranged between the sixth branch pipe and the ninth branch pipe.
6. The switchable catalyst dual fixed bed reactor according to claim 5, characterized in that: The eleventh branch pipe is also provided with a fifth branch pipe, one end of which is connected between the fourth branch pipe and the switch valve eight, one end of which is a regas outlet, and the fifth branch pipe is provided with a switch valve five.
7. The switchable catalyst dual fixed bed reactor according to claim 2, characterized in that: The product storage tank and the heat exchanger are connected by a pipeline, and a carrier gas outlet is arranged on the pipeline.
8. The switchable catalyst dual fixed bed reactor according to claim 6, characterized in that: The first air intake pipe and the eighth branch pipe are connected through the tenth branch pipe. The tenth branch pipe is arranged between the switch valve three and the switch valve eight. The tenth branch pipe is also provided with a switch valve ten.
9. The switchable catalyst dual fixed bed reactor according to claim 1, characterized in that: Solid catalysts are also fixed in the first reactor and the second reactor.
10. The switchable catalyst dual fixed bed reactor according to claim 8, characterized in that: The branch pipe and the air inlet pipe are made of stainless steel.