Device for reducing TPP consumption of butanol and octanol production system
By using a primary and secondary catalyst separation system and multiple separation processes, and by employing falling film evaporation, condensation, and absorption technologies, the problem of TPP being carried over during the production of butanol and octanol was solved, achieving efficient TPP recovery and cost reduction.
Patent Information
- Application Number
- CN202423203367.1
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-25
- Publication Date
- 2025-11-25
- Estimated Expiration
- 2034-12-25
AI Technical Summary
During the production of butanol and octanol, TPP is easily carried into downstream systems, leading to excessive consumption, energy waste, and increased production costs.
A primary and secondary catalyst separation system is adopted, combined with falling film evaporation, condensation and absorption technology, to recover TPP through four separation processes, including a first falling film evaporator, a catalyst separation tank, a condenser and a light component absorption tower, and a spray system and packing to improve separation efficiency.
It significantly improves the recycling rate of TPP, reduces the risk of TPP being carried into downstream systems, and lowers production costs.
Smart Images
Figure CN223587133U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to a device, concretely relates to a device for reducing the consumption of TPP in butanol production system belongs to chemical production technical field. BACKGROUND
[0002] In the production process of butanol, the separation and recovery of catalyst is a crucial step. Especially in the synthesis process, the reaction system often contains components such as carbonyl synthesis catalyst, TPP and mixed aldehyde. Because TPP has certain volatility and the characteristics of easy mixing with other components, it is often entrained to the downstream system in the separation process, resulting in excessive consumption of TPP, energy waste and increased production cost. SUMMARY
[0003] Based on the above background, the purpose of the utility model is to provide a device for reducing the consumption of TPP in butanol production system, which reduces the entrainment of TPP and improves the separation efficiency of catalyst, solving the problems in the background art.
[0004] In order to realize the above-mentioned utility model purpose, the utility model provides the following technical scheme:
[0005] A device for reducing the consumption of TPP in butanol production system, comprising a primary catalyst separation system, a catalyst separation tank, a first condenser, a secondary catalyst separation system, a catalyst separation tower, a second condenser, a storage tank, a light component absorption tower and a plurality of pipelines;
[0006] The primary catalyst separation system comprises a first falling film evaporator and a primary catalyst separation tank, and the secondary catalyst separation system comprises a second falling film evaporator and a secondary catalyst separation tank;
[0007] The first falling film evaporator is in communication with the primary catalyst separation tank through a pipeline;
[0008] The primary catalyst separation tank is in communication with the catalyst separation tank, the second falling film evaporator and the light component absorption tower through a pipeline;
[0009] The catalyst separation tank is in communication with the first condenser and the secondary catalyst separation tank through a pipeline;
[0010] The first condenser is in communication with the light component absorption tower through a pipeline;
[0011] The second falling film evaporator is in communication with the secondary catalyst separation tank through a pipeline;
[0012] The secondary catalyst separation tank is in communication with the catalyst separation tower through a pipeline;
[0013] The catalyst separation tower is communicated with the second condenser and the secondary catalyst separation tank through pipes;
[0014] The second condenser is communicated with the tank through pipes;
[0015] The tank is communicated with the light component absorption tower through pipes;
[0016] The pipes between the primary catalyst separation tank and the light component absorption tower are communicated with the catalyst separation tank and the secondary catalyst separation tank.
[0017] As a preferred, the secondary catalyst separation tank is further provided with a reflux channel, which is communicated with the secondary catalyst separation tank.
[0018] As a preferred, the light component absorption tower is further provided with a discharge channel, which is communicated with the light component absorption tower.
[0019] As a preferred, the temperature of the primary catalyst separation system is 85-110 DEG C; the pressure of the primary catalyst separation system is 1.2-1.5 MPag.
[0020] As a preferred, the temperature of the primary catalyst separation system is 100-135 DEG C; the pressure of the primary catalyst separation system is 0.69-0.71 MPag.
[0021] As a preferred, the temperature of the secondary catalyst separation system is 100-135 DEG C; the pressure of the secondary catalyst separation system is 0.69-0.71 MPag.
[0022] As a preferred, the catalyst separation tank is provided with a first spraying system.
[0023] As a preferred, the catalyst separation tower is provided with a filler and a second spraying system.
[0024] Compared with the prior art, the device has the following advantages:
[0025] The device for reducing the consumption of TPP in butanol production system of the utility model, through optimizing the separation process of catalyst, using falling film evaporation, condensation and absorption technology, significantly improve the recovery rate of TPP in the production of octanol, solve the problem that TPP is entrained into the downstream system. BRIEF DESCRIPTION OF DRAWINGS
[0026] To more clearly illustrate the technical solutions in the embodiments of this utility model or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only embodiments of this utility model. For those skilled in the art, other drawings can be obtained based on the provided drawings without creative effort.
[0027] Figure 1 This is a schematic diagram of the overall structure of this utility model.
[0028] In the diagram: 1. Primary catalyst separation system; 101. First falling film evaporator; 102. Primary catalyst separation receiving tank; 2. Catalyst separation tank; 3. First condenser; 4. Secondary catalyst separation system; 401. Second falling film evaporator; 402. Secondary catalyst separation receiving tank; 5. Catalyst separation tower; 6. Second condenser; 7. Storage receiving tank; 8. Light component absorption tower; 9. Reflux channel; 10. Discharge channel; 11. First spray system; 12. Packing material; 13. Second spray system. Detailed Implementation
[0029] The technical solution of this utility model will be further described in detail below through specific embodiments and in conjunction with the accompanying drawings. It should be understood that the implementation of this utility model is not limited to the following embodiments, and any modifications and / or alterations made to this utility model will fall within the protection scope of this utility model.
[0030] In this invention, unless otherwise specified, all parts and percentages are by weight, and the equipment and raw materials used are commercially available or commonly used in the field. Unless otherwise specified, the methods in the following embodiments are conventional methods in the field. Unless otherwise specified, the components or equipment in the following embodiments are general standard parts or components known to those skilled in the art, and their structures and principles can be learned by those skilled in the art through technical manuals or conventional experimental methods.
[0031] The embodiments of the present invention will be described in detail below with reference to the accompanying drawings. In the following detailed description, many specific details are set forth to facilitate explanation and provide a comprehensive understanding of the embodiments of the present invention. However, one or more embodiments may be practiced by those skilled in the art without these specific details.
[0032] like Figure 1 As shown, an apparatus for reducing TPP consumption in a butanol and octanol production system includes a primary catalyst separation system 1, a catalyst separation tank 2, a first condenser 3, a secondary catalyst separation system 4, a catalyst separation tower 5, a second condenser 6, a storage tank 7, a light component absorption tower 8, and several pipelines.
[0033] The primary catalyst separation system 1 comprises a first falling film evaporator 101 and a primary catalyst separation tank 102, and the secondary catalyst separation system 4 comprises a second falling film evaporator 401 and a secondary catalyst separation tank 402.
[0034] The temperature of the primary catalyst separation system 1 is 100-135℃. The pressure of the primary catalyst separation system 1 is 0.69-0.71 MPag.
[0035] The temperature of the secondary catalyst separation system 4 is 100-135℃. The pressure of the secondary catalyst separation system 4 is 0.69-0.71 MPag.
[0036] The temperature of the primary catalyst separation system 1 is 100-135℃. The pressure of the primary catalyst separation system 1 is 0.69-0.71 MPag.
[0037] The first falling film evaporator 101 is in communication with the primary catalyst separation tank 102 through a pipeline.
[0038] The primary catalyst separation tank 102 is in communication with the catalyst separation tank 2, the second falling film evaporator 401 and the light component absorption tower 8 through a pipeline, wherein the catalyst separation tank 2 is provided with a first spraying system 11.
[0039] The catalyst separation tank 2 is in communication with the first condenser 3 and the secondary catalyst separation tank 402 through a pipeline.
[0040] The first condenser 3 is in communication with the light component absorption tower 8 through a pipeline.
[0041] The second falling film evaporator 401 is in communication with the secondary catalyst separation tank 402 through a pipeline.
[0042] The secondary catalyst separation tank 402 is in communication with the catalyst separation tower 5 through a pipeline, wherein the catalyst separation tower 5 is provided with a filler 12 and a second spraying system 13.
[0043] The catalyst separation tower 5 is in communication with the second condenser 6 and the secondary catalyst separation tank 402 through a pipeline.
[0044] The second condenser 6 is in communication with the tank through a pipeline.
[0045] The tank is in communication with the light component absorption tower 8 through a pipeline.
[0046] The pipelines between the primary catalyst separation tank 102 and the light component absorption tower 8 are in communication with the catalyst separation tank 2 and the secondary catalyst separation tank 402.
[0047] The secondary catalyst separation tank 402 is further provided with a reflux channel 9, and the reflux channel 9 is in communication with the secondary catalyst separation tank 402.
[0048] The light component absorption tower 8 is also provided with a discharge channel 10 in communication with the light component absorption tower 8.
[0049] The implementation principle of the device for reducing the consumption of TPP in butanol production system is as follows:
[0050] Firstly, the mixed solution containing a carbonyl synthesis catalyst, TPP and mixed aldehyde is fed into the first catalyst separation system 1 from the micro-interface reaction system, wherein the feeding temperature of the mixed solution is 85-110 DEG C, and the feeding pressure is 1.2-1.5 MPag.
[0051] In the first catalyst separation system 1, the temperature is controlled between 100-135 DEG C, and the pressure is controlled between 0.69-0.71 MPag, and the mixed solution is preliminarily separated by the first falling film evaporator 101 and the first catalyst separation tank 102 through heating. The gaseous butyraldehyde and the mixture of a small amount of TPP enter the catalyst separation tank 2, at this time, the mixed aldehyde and the TPP are further separated in the catalyst separation tank 2, the first spraying system 11 is arranged in the catalyst separation tank 2, which is used for further washing the TPP in the gas phase, and the gas phase is condensed by the first condenser 3 and then enters the light component absorption tower 8, and the separated TPP enters the second catalyst separation tank 402 in the second catalyst separation system 4.
[0052] The liquid in the first catalyst separation system 1 is conveyed to the second catalyst separation system 4 through a pipeline in a sealed manner, and in the second catalyst separation system 4, the mixed solution is separated for the third time by the second falling film evaporator 401 and the second catalyst separation tank 402.
[0053] The concentrated catalyst in the second catalyst separation tank 402 returns to the upstream system of the device, and the mixture of gaseous butyraldehyde and a small amount of TPP enters the catalyst separation tower 5 for the fourth separation, the catalyst separation tower 5 is provided with the packing 12 and the second spraying system 13, the second spraying system 13 further washes the TPP in the gas phase, and the packing 12 can increase the contact area of the gas and the liquid. After the fourth separation, the TPP is recovered to the second catalyst separation tank 402 of the second catalyst separation system 4, and the gas phase is condensed by the condenser and then stored in the tank.
[0054] The mixed aldehyde separated by the first catalyst separation system 1 and the second catalyst separation system 4 enters the light component absorption tower 8, and the subsequent recovery and treatment are completed. Through the above separation process, the effective recovery of the TPP and the catalyst is ensured, and the risk of the TPP being entrained into the downstream system is reduced.
[0055] The principle and implementation mode of the present application are described by using specific examples in the present application, and the above examples are only used for helping to understand the method and core idea of the present application. It should be pointed out that, for ordinary skilled persons in the technical field, some improvements and modifications can be made to the present application without departing from the principle of the present application, and these improvements and modifications also fall within the protection scope of the present application.
Claims
1. A device for reducing the consumption of TPP in a butanol production system, characterized by: The device for reducing the consumption of TPP in the butanol production system comprises a first catalyst separation system (1), a catalyst separation tank (2), a first condenser (3), a second catalyst separation system (4), a catalyst separation column (5), a second condenser (6), a storage tank (7), a light component absorption column (8) and a plurality of pipelines. The first catalyst separation system (1) comprises a first falling film evaporator (101) and a first catalyst separation tank (102), and the second catalyst separation system (4) comprises a second falling film evaporator (401) and a second catalyst separation tank (402). The first falling film evaporator (101) is in communication with the first catalyst separation tank (102) through a pipeline. The first catalyst separation tank (102) is in communication with the catalyst separation tank (2), the second falling film evaporator (401) and the light component absorption column (8) through pipelines. The catalyst separation tank (2) is in communication with the first condenser (3) and the second catalyst separation tank (402) through pipelines. The first condenser (3) is in communication with the light component absorption column (8) through a pipeline. The second falling film evaporator (401) is in communication with the second catalyst separation tank (402) through a pipeline. The second catalyst separation tank (402) is in communication with the catalyst separation column (5) through a pipeline. The catalyst separation column (5) is in communication with the second condenser (6) and the second catalyst separation tank (402) through pipelines. The second condenser (6) is in communication with the storage tank through a pipeline. The storage tank is in communication with the light component absorption column (8) through a pipeline. The pipelines between the first catalyst separation tank (102) and the light component absorption column (8) are in communication with the catalyst separation tank (2) and the second catalyst separation tank (402).
2. The apparatus of claim 1, wherein: The second catalyst separation tank (402) is further provided with a reflux channel (9) in communication with the second catalyst separation tank (402).
3. The apparatus of claim 1, wherein: The light component absorption column (8) is further provided with a discharge channel (10) in communication with the light component absorption column (8).
4. The apparatus of claim 1, wherein: The feed temperature of the first catalyst separation system (1) is 85-110 ℃; and the feed pressure of the first catalyst separation system (1) is 1.2-1.5 MPag.
5. The apparatus of claim 1, wherein: The temperature of the first catalyst separation system (1) is 100-135 ℃; and the pressure of the first catalyst separation system (1) is 0.69-0.71 MPag.
6. The apparatus of claim 1, wherein: The temperature of the second catalyst separation system (4) is 100-135 ℃; and the pressure of the second catalyst separation system (4) is 0.69-0.71 MPag.
7. The apparatus of claim 1, wherein: The catalyst separation tank (2) is provided with a first spraying system (11).
8. The apparatus of claim 1, wherein: The catalyst separation column (5) is provided with a filler (12) and a second spraying system (13).