Energy-saving optimized butene isomerization production device
By using a thermally coupled process, the latent heat of the material at the top of the product refining tower is used to replace the steam heat energy, which solves the problem of high energy consumption in the raw material gasification process and achieves significant energy-saving effect and cost reduction.
Patent Information
- Application Number
- CN202423049159.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-12-11
- Publication Date
- 2025-11-04
- Estimated Expiration
- 2034-12-11
AI Technical Summary
In existing butene isomerization production facilities, the raw material gasification process consumes a lot of steam, resulting in high energy consumption and processing costs.
By employing a thermal coupling approach, a combination of components such as a raw material preheater, a raw material energy-saving vaporizer, a reaction feed heat exchanger, a reaction feed superheater, a heterogeneous reactor, a reaction product cooler, a gas-liquid separator, a gas compressor, and a product refining tower is used. This approach utilizes the latent heat of the material at the top of the product refining tower to replace part or all of the steam heat energy, thereby reducing the energy consumption of the raw material gasification process and reducing the consumption of circulating water through heat exchange.
It significantly reduces the consumption of steam and circulating water, lowers processing costs, and has a remarkable energy-saving effect. Overall energy consumption is reduced by about 30-50%, reducing enterprise production costs by about RMB 15.75 million per year and reducing carbon emissions by about 15,000 tons per year.
Smart Images
Figure CN223505271U_ABST
Abstract
Description
Technical Field
[0001] This utility model belongs to the field of chemical production technology, and in particular relates to an energy-saving and optimized butene isomerization production device. Background Technology
[0002] The butene isomerization unit uses C4 as raw material to isomerize n-butene in the C4 component into isobutene. Isobutene can be used as a raw material for the production of products such as tert-butanol, methyl tert-butyl ether, and flame retardants.
[0003] Butene isomerization is a gas-phase reaction, and the isomerization reactor requires gas-phase feed. The raw material C4 is in the liquid phase and needs to be heated and vaporized before it can enter the isomerization reactor. In the current industrial production process, low-pressure steam is used to heat and vaporize the raw material. The heating and vaporization section consumes a lot of steam, resulting in high energy consumption and processing costs for the entire project. Utility Model Content
[0004] In view of this, the present invention aims to provide an energy-saving and optimized butene isomerization production apparatus to solve at least one technical problem in the background art.
[0005] To achieve the above objectives, the technical solution of this utility model is implemented as follows:
[0006] An energy-saving and optimized butene isomerization production device includes a raw material gasification component, an isomerization reaction component, a separation and pressurization component, and a refining component;
[0007] The feedstock C4 is connected to the feedstock gasification unit, which is connected to the isomerization reaction unit, which is connected to the separation and pressurization unit, which is connected to the purification unit, and the purification unit exchanges heat with the feedstock gasification unit. The purification unit outputs isomerized C4.
[0008] Furthermore, the raw material gasification assembly includes a raw material preheater and a raw material energy-saving vaporizer;
[0009] The raw material C4 is connected to the raw material preheater, the raw material preheater is connected to the raw material energy-saving vaporizer, the raw material energy-saving vaporizer is connected to the heterogeneous reaction assembly, and the raw material energy-saving vaporizer exchanges heat with the refining assembly.
[0010] Furthermore, the heterogeneous reaction assembly includes a reaction feed heat exchanger, a reaction feed superheater, a heterogeneous reactor, and a reaction product cooler;
[0011] The reaction feed heat exchanger is connected to the raw material gasification assembly. The reaction feed heat exchanger, the reaction feed superheater, and the heterogeneous reactor are connected in sequence. The bottom of the heterogeneous reactor exchanges heat with the feed heat exchanger through a pipe, and then connects to the reaction product cooler through a pipe. The reaction product cooler is connected to the separation and pressurization assembly.
[0012] Furthermore, the separation and pressurization assembly includes a gas-liquid separator and a gas-generating compressor;
[0013] One side of the gas-liquid separator is connected to the heterogeneous reaction assembly, the top of the gas-liquid separator is connected to the gas-generating compressor, and the gas-generating compressor is connected to the refining assembly.
[0014] The bottom of the gas-liquid separator is connected to the refining components.
[0015] Furthermore, the refining components include a product refining column, a refining column top condenser, and a product refining column reflux tank;
[0016] The top of the product refining tower exchanges heat with the raw material gasification components through a pipeline, and then connects to the top condenser of the refining tower through another pipeline. The top condenser of the refining tower is connected to the product refining tower reflux tank. The bottom of the product refining tower reflux tank is connected to the top of the product refining tower. The bottom of the product refining tower reflux tank outputs isomeric C4.
[0017] Furthermore, the bottom of the product refining column outputs heavy components, the bottom of the product refining column is connected to the product refining column reboiler, and the product refining column reboiler is connected to one side of the product refining column.
[0018] Compared with existing technologies, the energy-saving and optimized butene isomerization production apparatus of this utility model has the following advantages:
[0019] 1. This application solves the problem of high energy consumption and large amount of heating steam in the raw material gasification process by adopting a thermal coupling method. Taking a 300,000-ton / year butene isomerization unit as an example, the above process can save about 51,000 tons / year of steam consumption and reduce processing costs by about 15 million yuan / year, with significant energy-saving effect.
[0020] 2. By adopting a thermal coupling method, this application not only solves the problem of large steam consumption in the raw material gasification process, but also reduces the circulating water consumption in the product refining process. Taking a 300,000-ton / year butene isomerization unit as an example, the above process can save about 2.52 million tons / year of circulating water consumption and reduce processing costs by about 750,000 yuan / year, which has a good energy-saving effect.
[0021] 3. Taking a 300,000-ton / year butene isomerization unit as an example, the energy consumption of the energy-saving process technology proposed in this application can be reduced by about 30-50%, and the processing cost can be reduced by about RMB 15.75 million / year. This not only significantly reduces the production cost of enterprises, but also reduces the carbon emissions of enterprises by about 15,000 tons / year, which is in line with the long-term strategic development policies of the country and enterprises. Attached Figure Description
[0022] The accompanying drawings, which form part of this utility model, are used to provide a further understanding of the utility model. The illustrative embodiments of the utility model and their descriptions are used to explain the utility model and do not constitute an undue limitation of the utility model. In the drawings:
[0023] Figure 1 This is a schematic diagram of an energy-saving and optimized butene isomerization production device according to an embodiment of the present invention.
[0024] Explanation of reference numerals in the attached figures:
[0025] 1. Raw material preheater; 2. Raw material energy-saving vaporizer; 3. Discharge heat exchanger; 4. Reactor feed superheater; 5. Heterogeneous reactor; 6. Reactor product cooler; 7. Gas-liquid separator; 8. Gas compressor; 9. Product refining tower; 10. Refining tower top condenser; 11. Product refining tower reflux tank; 12. Product refining tower reboiler. Detailed Implementation
[0026] It should be noted that, unless otherwise specified, the embodiments and features described in these embodiments can be combined with each other.
[0027] In the description of this utility model, it should be understood that the terms "center," "longitudinal," "lateral," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," and "outer," etc., indicating orientation or positional relationships based on the orientation or positional relationships shown in the accompanying drawings, are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model. Furthermore, the terms "first," "second," etc., are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of indicated technical features. Thus, features defined with "first," "second," etc., may explicitly or implicitly include one or more of that feature. In the description of this utility model, unless otherwise stated, "a plurality of" means two or more.
[0028] In the description of this utility model, it should be noted that, unless otherwise explicitly specified and limited, the terms "installation," "connection," and "joining" should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral connection; they can refer to a mechanical connection or an electrical connection; they can refer to a direct connection or an indirect connection through an intermediate medium; and they can refer to the internal connection of two components. Those skilled in the art can understand the specific meaning of the above terms in this utility model based on the specific circumstances.
[0029] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.
[0030] Example 1
[0031] An energy-saving and optimized butene isomerization production device includes a feed gasification component, an isomerization reaction component, a separation and pressurization component, and a refining component. The feed C4 is connected to the feed gasification component, the feed gasification component is connected to the isomerization reaction component, the isomerization reaction component is connected to the separation and pressurization component, the separation and pressurization component is connected to the refining component, the refining component exchanges heat with the feed gasification component, and the refining component outputs isomerized C4.
[0032] The raw material gasification assembly includes a raw material preheater 1 and a raw material energy-saving vaporizer 2. The raw material C4 is connected to the raw material preheater 1 through a pipeline, the raw material preheater 1 is connected to the raw material energy-saving vaporizer 2 through a pipeline, the raw material energy-saving vaporizer 2 is connected to the heterogeneous reaction assembly through a pipeline, and the raw material energy-saving vaporizer 2 exchanges heat with the refining assembly.
[0033] The heterogeneous reaction assembly includes a reaction feed heat exchanger 3, a reaction feed superheater 4, a heterogeneous reactor 5, and a reaction product cooler 6;
[0034] The reaction feed heat exchanger 3 is connected to the raw material gasification component via a pipeline. The reaction feed heat exchanger 3, the reaction feed superheater 4, and the heterogeneous reactor 5 are connected in sequence via pipelines. The bottom of the heterogeneous reactor 5 exchanges heat with the feed heat exchanger 3 via a pipeline, and then is connected to the reaction product cooler 6 via a pipeline. The reaction product cooler 6 is connected to the separation and pressurization component via a pipeline.
[0035] The separation and pressurization assembly includes a gas-liquid separator 7 and a gas-generating compressor 8; one side of the gas-liquid separator 7 is connected to the heterogeneous reaction assembly via a pipeline, the top of the gas-liquid separator 7 is connected to the gas-generating compressor 8 via a pipeline, the gas-generating compressor 8 is connected to the refining assembly via a pipeline, and the bottom of the gas-liquid separator 7 is connected to the refining assembly via a pipeline.
[0036] The refining assembly includes a product refining column 9, a refining column top condenser 10, and a product refining column reflux tank 11. The top of the product refining column 9 exchanges heat with the feed gasification assembly via a pipeline, and is then connected to the refining column top condenser 10 via another pipeline. The refining column top condenser 10 is connected to the product refining column reflux tank 11 via a pipeline. The bottom of the product refining column reflux tank 11 outputs isomeric C4. The bottom of the product refining column 9 outputs heavy components. The bottom of the product refining column 9 is connected to the product refining column reboiler 12 via a pipeline, and the product reboiler 12 is connected to one side of the product refining column 9 via a pipeline.
[0037] The gaseous isomerized C4 component is collected from the top of the product refining tower 9 and enters the tube side of the feed vaporizer 2. The material from the outlet of the feed vaporizer 2 enters the top condenser 10 of the product refining tower. Finally, the gaseous isomerized C4 component becomes a liquid phase and enters the product refining tower reflux tank 11. Part of the material at the bottom of the reflux tank 11 is returned to the product refining tower 9 as reflux, and part is sent outside the unit as product. The feed C4 is completely converted into a gaseous material after being heated in the feed vaporizer 2, and then enters the subsequent isomerization reaction process.
[0038] The gaseous isomeric C4 component at the top of the product refining tower 9 exchanges heat with the raw material C4 in the raw material vaporizer 2, making full use of the latent heat of phase change of the gaseous isomeric C4 component. This latent heat of phase change can completely or partially replace the heat energy of the heating steam, thereby reducing the amount of steam used and reducing energy consumption. At the same time, it reduces the cooling load of the gaseous isomeric C4 component at the top of the product refining tower 9, thereby reducing the amount of circulating water used.
[0039] The operating pressure of the product refining tower 9 is 0.3~1.0 MPaG, the operating temperature is 50~180℃, and the outlet temperature of the raw material vaporizer 2 (raw material C4 side) is 45~60℃.
[0040] Example 2:
[0041] Raw material gasification process: The raw material C4 is pressurized by a pump and sent to the raw material gasification process. It exchanges heat with steam condensate in the raw material preheater 1. After the heat exchange and temperature increase, it enters the raw material energy-saving vaporizer 2. The raw material C4 is heated and gasified and then enters the isomerization reaction process.
[0042] Isomerization reaction process: The gasified raw material C4 exchanges heat with the reaction products in the reaction feed heat exchanger 3 and then enters the reaction feed superheater 4. After being superheated to the reaction temperature, it enters the isomerization reactor 5. The reaction products finally enter the reaction product cooler 6 and are cooled to 40°C before entering the gas-liquid separator 7. The gas phase material at the top of the gas-liquid separator 7 is pressurized by the gas generator compressor 8 and then enters the product refining tower 9 together with the liquid phase material.
[0043] Product refining process: The reaction product enters the product refining tower 9, the top material enters the raw material energy-saving heat exchanger 2, and after heat exchange, it enters the top condenser 10 of the product refining tower. After cooling, it enters the product refining tower reflux tank 11. Part of the material at the bottom of the tank enters the product refining tower 9, and part of it is sent out of the production unit as product isomeric C4. The bottom material of the product refining tower 9 is sent out of the production unit as heavy component.
[0044] Table 1 shows the main process operation parameters.
[0045] Serial Number Process Equipment Name Operating parameters 1 Raw material gasification process Raw material energy-saving gasifier 2 50℃, 0.4MPaG 2 Isomerization process Heterogeneous reactor 5 0.1 MPaG, 350℃ 3 Product refining process Product Refining Tower 9 0.6 MPaG, 60℃
[0046] Based on the process flow of Implementation Case 1 and the operating parameters in Table 1, taking a 300,000-ton / year butene isomerization unit as an example, the heat load of the raw material energy-saving gasifier in the raw material gasification process is reduced by about 3,100 kW, which is equivalent to the heat energy generated by 5.0 tons of steam. Based on 8,000 hours of production time per year, the annual steam saving is 40,000 tons / year, and the processing cost is reduced by about 12 million yuan / year.
[0047] Example 3:
[0048] Compared with Example 1, Example 3 does not change the process flow, only the operating pressure of the product refining process is changed.
[0049] Table 2 shows the main process operation parameters.
[0050] Serial Number Process Equipment Name Operating parameters 1 Raw material gasification process Raw material energy-saving gasifier 2 50℃, 0.4MPaG 2 Isomerization process Heterogeneous reactor 5 0.1 MPaG, 350℃ 3 Product refining process Product Refining Tower 9 0.65 MPaG, 65℃
[0051] Based on the process flow of Implementation Case 1 and the operating parameters in Table 2, taking a 300,000-ton / year butene isomerization unit as an example, the heat load of the raw material energy-saving gasifier in the raw material gasification process is reduced by about 3,800 kW, which is equivalent to the heat energy generated by 6.5 tons of steam. Based on 8,000 hours of production time per year, the annual steam saving is 52,000 tons / year, and the processing cost is reduced by about 15.6 million yuan / year.
[0052] This application utilizes thermal coupling to fully leverage the latent heat of the material at the top of the product refining tower, using this latent heat as heating energy for the raw material gasification process, thereby achieving the goal of completely or partially replacing steam heat energy and reducing energy consumption.
[0053] After the gaseous material at the top of the product refining tower exchanges heat with the raw material, most of the gaseous material at the top of the tower becomes liquid, which reduces the cooling load of the subsequent condenser, thereby reducing the amount of circulating water used and reducing energy consumption.
[0054] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.
Claims
1. An energy-saving and optimized butene isomerization production apparatus, characterized in that: Includes raw material gasification components, heterogeneous reaction components, separation and pressurization components, and refining components; The feedstock C4 is connected to the feedstock gasification unit, which is connected to the isomerization reaction unit, which is connected to the separation and pressurization unit, which is connected to the purification unit, and the purification unit exchanges heat with the feedstock gasification unit. The purification unit outputs isomerized C4.
2. The energy-saving and optimized butene isomerization production apparatus according to claim 1, characterized in that: The raw material gasification assembly includes a raw material preheater and a raw material energy-saving vaporizer; The raw material C4 is connected to the raw material preheater, the raw material preheater is connected to the raw material energy-saving vaporizer, the raw material energy-saving vaporizer is connected to the heterogeneous reaction assembly, and the raw material energy-saving vaporizer exchanges heat with the refining assembly.
3. The energy-saving and optimized butene isomerization production apparatus according to claim 1, characterized in that: The heterogeneous reaction assembly includes a reaction feed heat exchanger, a reaction feed superheater, a heterogeneous reactor, and a reaction product cooler; The reaction feed heat exchanger is connected to the raw material gasification assembly. The reaction feed heat exchanger, the reaction feed superheater, and the heterogeneous reactor are connected in sequence. The bottom of the heterogeneous reactor exchanges heat with the feed heat exchanger through a pipe, and then connects to the reaction product cooler through a pipe. The reaction product cooler is connected to the separation and pressurization assembly.
4. The energy-saving and optimized butene isomerization production apparatus according to claim 1, characterized in that: The separation and pressurization assembly includes a gas-liquid separator and a gas-generating compressor; One side of the gas-liquid separator is connected to the heterogeneous reaction assembly, the top of the gas-liquid separator is connected to the gas-generating compressor, and the gas-generating compressor is connected to the refining assembly. The bottom of the gas-liquid separator is connected to the refining components.
5. The energy-saving and optimized butene isomerization production apparatus according to claim 1, characterized in that: The refining components include a product refining column, a refining column top condenser, and a product refining column reflux tank; The top of the product refining tower exchanges heat with the raw material gasification components through a pipeline, and then connects to the top condenser of the refining tower through another pipeline. The top condenser of the refining tower is connected to the product refining tower reflux tank. The bottom of the product refining tower reflux tank is connected to the top of the product refining tower. The bottom of the product refining tower reflux tank outputs isomeric C4.
6. The energy-saving and optimized butene isomerization production apparatus according to claim 5, characterized in that: The bottom of the product refining column outputs heavy components. The bottom of the product refining column is connected to the reboiler of the product refining column, and the reboiler of the product refining column is connected to one side of the product refining column.