Ammoximation reaction heat recovery device
By designing a heat recovery device for the ammonium oxime reaction, a compressor is used to raise the working fluid temperature and recycle the reaction heat. This solves the problems of low temperature and difficulty in heat extraction in the utilization of heat from the cyclohexanone ammonium oxime reaction, and achieves efficient recycling of reaction heat and reduced energy consumption.
Patent Information
- Application Number
- CN202520064122.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-01-10
- Publication Date
- 2025-12-30
- Estimated Expiration
- 2035-01-10
AI Technical Summary
The utilization of the heat of reaction in the amination of cyclohexanone faces the problems of low temperature and difficulty in direct heat extraction, especially since the presence of catalyst in the circulating reaction solution can easily lead to pipeline blockage.
Design a heat recovery device for ammonia oximation reaction, which utilizes the heat from the ammonia oximation reaction to gasify the working fluid and raises the working fluid temperature through a compressor to supply the heat to the heaters in the device. The device includes a combination of components such as an ammonia oximation reactor, a reaction heat extractor, a working fluid tank, a compressor, and a heat exchanger.
It effectively solves the problems of low material temperature and difficulty in direct heat extraction, realizes the recycling of heat from ammonia oxime reaction, reduces energy consumption and carbon emissions of the unit, and avoids the risk of catalyst blockage.
Smart Images
Figure CN223741032U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to the field of reaction heat recovery, specifically relates to a kind of ammonium oxime reaction heat recovery device. BACKGROUND
[0002] Cyclohexanone ammonium oxime reaction is the exothermic reaction of cyclohexanone, hydrogen peroxide and ammonia to generate cyclohexanone oxime, and the reaction heat is about 300 kJ / mol. If this part of the reaction heat can be used to heat other process media, it will greatly reduce the energy consumption and carbon emissions of the device, and produce huge economic and social benefits. However, since the cyclohexanone ammonium oxime reaction temperature is only 80-100℃, the utilization of reaction heat faces the problem of low temperature level.
[0003] CN217092122U discloses a device for heating a benzene distillation column using heterogeneous cyclohexanone ammonium oxime reaction heat. The device uses heterogeneous cyclohexanone ammonium oxime reaction circulating liquid to heat the benzene distillation column, while also removing the reaction heat.
[0004] However, the current cyclohexanone ammonium oxime reaction circulating liquid contains catalyst, which is directly introduced into the benzene distillation column preheater, which can easily cause catalyst blockage in the pipeline and low temperature of the circulating reaction liquid. Therefore, a new reaction heat recovery device is needed. SUMMARY
[0005] The utility model aims to overcome the problem of low temperature of the circulating reaction liquid containing catalyst in the prior art, and provide an ammonium oxime reaction heat recovery device, which effectively solves the problem of low temperature of the material and difficulty in direct heat extraction, and effectively recycles the reaction heat.
[0006] To achieve the above purpose, the utility model provides an ammonium oxime reaction heat recovery device, which comprises an ammonium oxime reactor 1, a reaction heat extractor 3, a working medium tank 4, a compressor 6 and a heat exchanger 7.
[0007] The reaction heat extractor 3 comprises a hot side and a cold side, the liquid phase outlet of the ammonium oxime reactor 1 is communicated with the hot side inlet of the reaction heat extractor 3, and the hot side outlet of the reaction heat extractor 3 is communicated with the ammonium oxime reactor 1.
[0008] The liquid phase outlet of the working medium tank 4 is communicated with the cold side inlet of the reaction heat extractor 3, the cold side outlet of the reaction heat extractor 3 is communicated with the inlet of the compressor 6, the outlet of the compressor 6 is communicated with the hot side inlet of the heat exchanger 7, and the hot side outlet of the heat exchanger 7 is communicated with the inlet of the working medium tank 4.
[0009] Optionally, the device further comprises a reaction circulating pump 2, the liquid phase outlet of the ammoximation reactor 1 is communicated with the inlet of the reaction circulating pump 2, and the outlet of the reaction circulating pump 2 is communicated with the hot side inlet of the reaction heat exchanger 3.
[0010] Optionally, a gas-liquid separation tank 8 is arranged between the cold side outlet of the reaction heat exchanger 3 and the inlet of the compressor 6.
[0011] Optionally, a heater 9 is arranged between the reaction heat exchanger 3 and the compressor 6, for improving the inlet temperature of the compressor 6.
[0012] Optionally, a return line is arranged between the outlet and the inlet of the compressor 6, for improving the inlet temperature of the compressor 6.
[0013] The reaction heat exchanger 3 is connected in parallel with a heater, the cold side inlet of the heater is communicated with the outlet of the working medium circulating pump 5, and the cold side outlet of the heater is communicated with the inlet of the compressor 6.
[0014] Optionally, the device further comprises a working medium circulating pump 5, the liquid phase outlet of the working medium tank 4 is communicated with the inlet of the working medium circulating pump 5, and the outlet of the working medium circulating pump 5 is communicated with the cold side inlet of the reaction heat exchanger 3.
[0015] Optionally, the gas phase outlet of the working medium tank 4 is communicated with the cold side outlet of the reaction heat exchanger 3, for sending the gas phase in the working medium tank 4 into the compressor 6.
[0016] Optionally, the compressor 6 is a centrifugal compressor and / or a reciprocating compressor.
[0017] Optionally, the device further comprises an ammoximation reaction raw material unit 10, the outlet of the ammoximation reaction raw material unit 10 is connected with the inlet of the ammoximation reactor 1, for delivering ammoximation reaction raw materials to the ammoximation reactor 1.
[0018] Through the above technical scheme, the beneficial effects are as follows:
[0019] The reaction heat recovery device provided by the utility model utilizes ammoximation reaction heat gasification working medium, and utilizes the compressor to compress the gasification working medium to improve the working medium temperature level, supplies the heat to each heater of the device, solves the problem of low material temperature level and direct heat taking difficulty, and effectively circulates and reuses the ammoximation reaction heat. ACCURACY OF DRAWINGS
[0020] Figure 1 It is the basic schematic view of the ammoximation reaction heat recovery device provided by the utility model;
[0021] Figure 2 It is the detailed schematic view of the ammoximation reaction heat recovery device provided by the utility model.
[0022] Reference Signs List
[0023] 1-ammonia oximation reactor 2-reaction circulating pump 3-reaction heat extractor
[0024] 4-working medium tank 5-working medium circulating pump 6-compressor
[0025] 7-heat exchanger 8-gas-liquid separation tank 9-heater
[0026] 10-ammonia oximation reaction raw material unit DETAILED DESCRIPTION
[0027] The endpoints of the ranges and any values disclosed herein are not limited to the precise values recited as the exact dimensions are not critical to the properties. The endpoints of the ranges and any numerical values should be interpreted as approximately as the range of values in and about the ends points as they will vary slightly depending on how the range is assessed. For numerical ranges having an upper and lower end, the endpoints are included in the range.
[0028] In the present utility model, in the case that no opposite statement is made, the orientation words such as "up, down, left, right" generally refer to the orientation shown in the drawing. "Inner, outer" refers to the inner and outer relative to the outline of each component.
[0029] The utility model provides a kind of ammonia oximation reaction heat recovery device, the device includes ammonia oximation reactor 1, reaction heat extractor 3, working medium tank 4, compressor 6, heat exchanger 7;
[0030] Wherein, the reaction heat extractor 3 includes hot side and cold side, the liquid phase outlet of the ammonia oximation reactor 1 is communicated with the hot side inlet of reaction heat extractor 3, and the hot side outlet of reaction heat extractor 3 is communicated with the ammonia oximation reactor 1;
[0031] The liquid phase outlet of the working medium tank 4 is communicated with the cold side inlet of reaction heat extractor 3, the cold side outlet of reaction heat extractor 3 is communicated with the inlet of compressor 6, the outlet of compressor 6 is communicated with the hot side inlet of heat exchanger 7, and the hot side outlet of heat exchanger 7 is communicated with the inlet of working medium tank 4.
[0032] In the present utility model, the reaction heat recovery device provided utilizes ammonia oximation reaction hot gasification working medium, and utilizes compressor to compress gasification working medium to promote working medium temperature level, to supply heat to each heat exchanger of device, solve the problem that material temperature level is low and direct heat extraction is difficult, and effectively recycle reaction heat of ammonia oximation reaction.
[0033] According to a preferred embodiment of the present utility model, Figure 1The oximation reaction is carried out in the oximation reactor 1 to obtain an oximation reaction product, and the oximation reaction condition is not particularly limited, and those skilled in the art can adaptively adjust the reaction condition of the oximation reaction.
[0034] According to a preferred embodiment of the utility model, the device further comprises a reaction circulating pump 2, the liquid phase outlet of the oximation reactor 1 is communicated with the inlet of the reaction circulating pump 2, and the outlet of the reaction circulating pump 2 is communicated with the hot side inlet of the reaction heat exchanger 3. The oximation reaction product is sent into the reaction heat exchanger 3 by the reaction circulating pump 2, and the type of the reaction circulating pump is not particularly limited, and those skilled in the art can select the circulating pump of the prior art according to the oximation reaction condition.
[0035] According to a preferred embodiment of the utility model, the reaction heat exchanger 3 comprises a hot side and a cold side, the oximation reaction product is introduced into the hot side, and the working medium is introduced into the cold side, and heat exchange is carried out in the reaction heat exchanger 3 to effectively recycle the reaction heat of the oximation reaction.
[0036] According to a preferred embodiment of the utility model, a gas-liquid separation tank 8 is arranged between the cold side outlet of the reaction heat exchanger 3 and the inlet of the compressor 6.
[0037] According to a preferred embodiment of the utility model, a heater 9 is arranged between the reaction heat exchanger 3 and the compressor 6 to improve the inlet temperature of the compressor 6.
[0038] In the utility model, when the gas-liquid separation tank 8 and the heater 9 are arranged in the device at the same time, the connection order of the gas-liquid separation tank 8 and the heater 9 is not particularly limited, and according to the flow direction of the working medium, the working medium can be buffered by the gas-liquid separation tank first and then further gasified by the heater, or the working medium can be first passed through the heater and then passed through the gas-liquid separation tank to ensure that there is no liquid in the gasified working medium.
[0039] According to a preferred embodiment of the utility model, a return line is arranged between the outlet and the inlet of the compressor 6 to improve the inlet temperature of the compressor 6.
[0040] According to a preferred embodiment of the utility model, the type of the compressor is not particularly limited, and preferably the compressor 6 is a centrifugal compressor and / or a reciprocating compressor. Those skilled in the art can adaptively adjust the compression power and the air extraction amount of the compressor according to the gasification heat generation condition of the working medium after heat exchange, compress the working medium after heat exchange and gasification of the reaction heat exchanger 3, improve the temperature level of the working medium, and supply the heat to the heat exchangers of the device.
[0041] According to a preferred embodiment of the utility model, the device further comprises a working medium circulating pump 5, the liquid phase outlet of the working medium tank 4 is in communication with the inlet of the working medium circulating pump 5, and the outlet of the working medium circulating pump 5 is in communication with the cold side inlet of the reaction heat extractor 3.
[0042] According to a preferred embodiment of the utility model, the reaction heat extractor 3 is connected in parallel with a heater (not shown in the figure), the cold side inlet of the heater is in communication with the outlet of the working medium circulating pump 5, and the cold side outlet of the heater is in communication with the inlet of the compressor 6.
[0043] According to a preferred embodiment of the utility model, the gas phase outlet of the working medium tank 4 is in communication with the cold side outlet of the reaction heat extractor 3, for sending the gas phase in the working medium tank 4 into the compressor 6. Optionally, the working medium after heat exchange through the heat exchanger 7 is circulated back to the working medium tank 4, and due to the decrease in pressure, the working medium in the working medium tank may be gasified, so the gas phase outlet pipeline of the working medium tank 4 is connected with the cold side outlet pipeline of the reaction heat extractor 3, and a small amount of gasified working medium enters the compressor 6 through the pipeline, thereby reducing heat consumption.
[0044] According to a preferred embodiment of the utility model, the working medium is the compression medium of the compressor, and the type of the working medium in the working medium tank 4 can be selected from a wide range, which is a conventional medium that is gasified after heat exchange with the oximation reaction product in the field.
[0045] According to a preferred embodiment of the utility model, the above working medium is subjected to heat exchange with the oximation reaction product, the working medium is gasified under the action of the heat of the oximation reaction, the heat of the oximation reaction is effectively transferred to the working medium, the heat is used in the heat exchanger connected to the outlet of the compressor after compression, the recycling of the heat of the oximation reaction is realized, and the problems of difficulty in direct heat extraction and selection of the working medium are solved.
[0046] According to a preferred embodiment of the utility model, the heat exchanger 7 is a conventional heat exchanger with heating requirement in the field, and the number of the heat exchanger 7 is not particularly limited, and the number of the heat exchanger can be adaptively adjusted by the person skilled in the art according to the heat recovery condition of the outlet of the compressor 6, and the number of the heat exchanger 7 is at least 1.
[0047] According to a preferred embodiment of the utility model, the application field of the heat exchanger 7 is not particularly limited, and the heat exchanger 7 can be a conventional reboiler, for example, the heat exchanger can be a separation column reboiler.
[0048] According to a preferred embodiment of the utility model, the device further comprises an ammoximation reaction raw material unit 10, the outlet of the ammoximation reaction raw material unit 10 is connected with the inlet of the ammoximation reactor 1, and is used to deliver ammoximation reaction raw material to the ammoximation reactor 1. The utility model is not particularly limited to the ammoximation reaction raw material, and is the conventional ammoximation reaction raw material in the art, preferably cyclohexanone.
[0049] According to some specific embodiments of the utility model, as shown in Figure 1 and Figure 2 shown, the reaction heat recovery device is used to recycle the reaction heat, the ammoximation reaction raw material unit 10 is used to deliver the ammoximation reaction raw material to the ammoximation reactor 1, the ammoximation reaction is carried out to obtain the ammoximation reaction product, the reaction circulation pump 2 is used to deliver the ammoximation reaction product to the reaction heat exchanger 3 to exchange heat with the working medium, the ammoximation reaction product after heat exchange is circulated back to the ammoximation reactor 1 through the hot side outlet of the reaction heat exchanger 3
[0050] The working medium in the working medium tank 4 is delivered to the reaction heat exchanger 3 through the working medium circulation pump 5 to exchange heat, the gaseous working medium is delivered to the compressor 6, is compressed by the compressor 6, and is delivered to the heat exchanger 7 to further use the heat in different fields.
[0051] According to some preferred embodiments of the utility model, as shown in Figure 2 the working medium after heat exchange in the reaction heat exchanger 3 is delivered to the compressor 6 after passing through the gas-liquid separation tank 8 and the heater 9, is compressed, and is delivered to the heat exchanger 7.
[0052] The utility model will be described in detail through examples and comparative examples below. In the following examples and comparative examples, unless otherwise specified, the reagents used in the utility model are commercially available.
[0053] Example 1
[0054] The embodiment provides a device for separating toluene and cyclohexanone oxime by using ammoximation reaction heat, as shown in Figure 1 .
[0055] The ammoximation reaction raw material unit 10 is used to deliver the ammoximation reaction raw material to the ammoximation reactor 1, the ammoximation reaction is carried out to obtain the ammoximation reaction product, the liquid phase outlet of the ammoximation reactor 1 is communicated with the inlet of the reaction circulation pump 2, the outlet of the reaction circulation pump 2 is communicated with the hot side inlet of the reaction heat exchanger 3, the ammoximation reaction product is delivered to the reaction heat exchanger 3 through the reaction circulation pump 2, exchanges heat with the working medium, and then enters the ammoximation reactor 1 through the hot side outlet of the reaction heat exchanger 3.
[0056] The liquid phase outlet of the working medium tank 4 is communicated with the inlet of the working medium circulating pump 5, the outlet of the working medium circulating pump 5 is communicated with the cold side inlet of the reaction heat exchanger 3, the cold side outlet of the reaction heat exchanger 3 is communicated with the inlet of the compressor 6, the working medium is introduced into the compressor 6 by the working medium circulating pump 5 to exchange heat with the ammoximation reaction product, the outlet of the compressor 6 is communicated with the hot side inlet of the heat exchanger 7, the heat exchanger 7 is a toluene oxime separation tower reboiler, the hot side outlet of the heat exchanger 7 is communicated with the inlet of the working medium tank 4, and the heat-exchanged working medium returns to the working medium tank 4 for circulation.
[0057] The feed amount of the toluene oxime separation tower is 40 t / h, the mass fractions of toluene and cyclohexanone oxime in the toluene oxime are 62 wt% and 38 wt% respectively, the overhead discharge is toluene, the bottom discharge is toluene oxime concentrate, and the mass fractions of toluene and cyclohexanone oxime in the toluene oxime concentrate are 24 wt% and 76 wt% respectively.
[0058] Example 2
[0059] This embodiment provides a device for separating ammonia in wastewater by utilizing the heat of ammoximation reaction, as shown in Figure 1 .
[0060] The ammoximation reaction raw material is sent to the ammoximation reactor 1 by the ammoximation reaction raw material unit 10, the ammoximation reaction is carried out to obtain an ammoximation reaction product, the liquid phase outlet of the ammoximation reactor 1 is communicated with the inlet of the reaction circulating pump 2, the outlet of the reaction circulating pump 2 is communicated with the hot side inlet of the reaction heat exchanger 3, the ammoximation reaction product is sent to the reaction heat exchanger 3 by the reaction circulating pump 2, exchanges heat with the working medium, and then enters the ammoximation reactor 1 through the hot side outlet of the reaction heat exchanger 3.
[0061] The liquid phase outlet of the working medium tank 4 is communicated with the inlet of the working medium circulating pump 5, the outlet of the working medium circulating pump 5 is communicated with the cold side inlet of the reaction heat exchanger 3, the cold side outlet of the reaction heat exchanger 3 is communicated with the inlet of the compressor 6, the working medium is introduced into the compressor 6 by the working medium circulating pump 5 to exchange heat with the ammoximation reaction product, the outlet of the compressor 6 is communicated with the hot side inlet of the heat exchanger 7, the heat exchanger 7 is a toluene oxime separation tower reboiler, the hot side outlet of the heat exchanger 7 is communicated with the inlet of the working medium tank 4, and the heat-exchanged working medium returns to the working medium tank 4 for circulation.
[0062] The wastewater feed amount of the deamination tower is 30 t / h, and the mass fraction of ammonia is 5 wt%, the overhead discharge is ammonia water with a mass fraction of 25 wt% of ammonia, and the bottom discharge is wastewater substantially free of ammonia.
[0063] The preferred embodiments of the present application are described in detail above, but the present application is not limited thereto. Within the technical concept of the present application, various simple modifications can be made to the technical solution of the present application, including the combination of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as disclosed content of the present application, and all belong to the protection scope of the present application.
Claims
1. An apparatus for recovering heat from an ammoximation reaction, characterized by The device comprises an ammoximation reactor (1), a reaction heat exchanger (3), a working medium tank (4), a compressor (6), a heat exchanger (7); The reaction heat exchanger (3) comprises a hot side and a cold side, the liquid phase outlet of the ammoximation reactor (1) is communicated with the hot side inlet of the reaction heat exchanger (3), and the hot side outlet of the reaction heat exchanger (3) is communicated with the ammoximation reactor (1). The liquid phase outlet of the working medium tank (4) is communicated with the cold side inlet of the reaction heat exchanger (3), the cold side outlet of the reaction heat exchanger (3) is communicated with the inlet of the compressor (6), the hot side outlet of the heat exchanger (7) is communicated with the inlet of the working medium tank (4).
2. The apparatus of claim 1, wherein, The device further comprises a reaction circulating pump (2), the liquid phase outlet of the ammoximation reactor (1) is communicated with the inlet of the reaction circulating pump (2), and the outlet of the reaction circulating pump (2) is communicated with the hot side inlet of the reaction heat exchanger (3).
3. The apparatus of claim 1, wherein, A gas-liquid separation tank (8) is arranged between the cold side outlet of the reaction heat exchanger (3) and the inlet of the compressor (6).
4. The apparatus of claim 1, wherein, A heater (9) is arranged between the reaction heat exchanger (3) and the compressor (6) to increase the inlet temperature of the compressor (6).
5. The apparatus of claim 1, wherein, A return line is arranged between the outlet and the inlet of the compressor (6) to increase the inlet temperature of the compressor (6).
6. The apparatus of claim 1 or 5, wherein, The reaction heat exchanger (3) is connected in parallel with a heater, the cold side inlet of the heater is communicated with the outlet of the working medium circulating pump (5), and the cold side outlet of the heater is communicated with the inlet of the compressor (6).
7. The apparatus of claim 1, wherein, The gas phase outlet of the working medium tank (4) is communicated with the cold side outlet of the reaction heat exchanger (3) to send the gas phase in the working medium tank (4) into the compressor (6).
8. The apparatus of claim 1, wherein, The device further comprises a working medium circulating pump (5), the liquid phase outlet of the working medium tank (4) is communicated with the inlet of the working medium circulating pump (5), and the outlet of the working medium circulating pump (5) is communicated with the cold side inlet of the reaction heat exchanger (3).
9. The apparatus of claim 1, wherein, The compressor (6) is a centrifugal compressor and / or a reciprocating compressor.
10. The apparatus of claim 1, wherein, The device further comprises an ammoximation reaction raw material unit (10), the outlet of the ammoximation reaction raw material unit (10) is connected with the inlet of the ammoximation reactor (1) to deliver ammoximation reaction raw materials to the ammoximation reactor (1).