CN220090530U - Cyclohexanol knockout tower and cyclohexanol rectifying column economizer system - Google Patents
Cyclohexanol knockout tower and cyclohexanol rectifying column economizer system Download PDFInfo
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- CN220090530U CN220090530U CN202321574652.7U CN202321574652U CN220090530U CN 220090530 U CN220090530 U CN 220090530U CN 202321574652 U CN202321574652 U CN 202321574652U CN 220090530 U CN220090530 U CN 220090530U
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- cyclohexanol
- tower
- rectifying tower
- outlet
- cooler
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- HPXRVTGHNJAIIH-UHFFFAOYSA-N cyclohexanol Chemical compound OC1CCCCC1 HPXRVTGHNJAIIH-UHFFFAOYSA-N 0.000 title claims abstract description 264
- 238000000926 separation method Methods 0.000 claims abstract description 52
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 claims abstract description 42
- 230000036571 hydration Effects 0.000 claims abstract description 21
- 238000006703 hydration reaction Methods 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000010992 reflux Methods 0.000 claims description 44
- 239000012071 phase Substances 0.000 claims description 28
- 238000000605 extraction Methods 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 5
- 239000008346 aqueous phase Substances 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 abstract description 6
- 238000000034 method Methods 0.000 abstract description 6
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 2
- 230000008878 coupling Effects 0.000 abstract 1
- 238000010168 coupling process Methods 0.000 abstract 1
- 238000005859 coupling reaction Methods 0.000 abstract 1
- 239000000126 substance Substances 0.000 description 6
- WNLRTRBMVRJNCN-UHFFFAOYSA-N adipic acid Chemical compound OC(=O)CCCCC(O)=O WNLRTRBMVRJNCN-UHFFFAOYSA-N 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 235000011037 adipic acid Nutrition 0.000 description 2
- 239000001361 adipic acid Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000543 intermediate Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- 229920002292 Nylon 6 Polymers 0.000 description 1
- 229920002302 Nylon 6,6 Polymers 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a cyclohexanol separating tower and cyclohexanol rectifying tower energy-saving system, wherein the product cyclohexanol coming out of a cyclohexanol No. 1 cooler has a certain amount of heat, and the cyclohexanol No. 2 cooler is required to be used for continuous cooling, so that a certain amount of circulating cooling water is consumed in the period. At the same time, since cyclohexene exiting the bubble cap layer of the cyclohexanol separation column needs to be preheated before it can enter the hydration reactor, a certain amount of heat is consumed during this period to preheat it. Both of the above processes result in increased amounts of circulating water and increased heat source supply, which can result in wasted utility. According to the utility model, the high-temperature cyclohexanol product discharged from the middle part of the cyclohexanol rectifying tower through the cyclohexanol 1# cooler and cyclohexene discharged from the bubble cap layer of the cyclohexanol separating tower to the hydration reactor are subjected to heat exchange, and cold and hot materials transfer heat mutually, so that the coupling of heat is realized, the unit consumption of cyclohexanol production is finally reduced, and the production cost is saved.
Description
Technical Field
The utility model belongs to the field of energy-saving optimization and transformation of chemical steam, and particularly relates to an energy-saving system of a cyclohexanol separating tower and a cyclohexanol rectifying tower.
Background
Cyclohexanol is an important organic intermediate, and can be used for synthesis of pesticides, dyes, drug intermediates and the like, and is also a main raw material for preparing caprolactam and adipic acid, wherein caprolactam and adipic acid are important raw materials for producing nylon 66 and nylon 6. The traditional synthesis method of cyclohexanol comprises three phenol hydrogenation reduction methods, cyclohexane oxidation methods and cyclohexene hydration methods, and the Henan Ma Nilong chemical industry Limited company adopts the cyclohexene hydration method to produce cyclohexanol. The development speed of the chemical industry in recent years is faster, and the energy conservation and consumption reduction become the important problems in the chemical industry. However, the cyclohexanol product coming out of the middle part of the cyclohexanol rectifying tower in actual production still has higher temperature after heat exchange by a cyclohexanol 1# cooler, a certain amount of circulating cooling water is required to be consumed in the period of cooling by the cyclohexanol 2# cooler, the heat is not fully utilized, and meanwhile cyclohexene coming out of a cyclohexanol separating tower bubble cap layer and entering a hydration reactor needs to be preheated, a certain heat source is required to be consumed in preheating, and a certain heat energy source and energy consumption exist. Along with the increasing importance of energy source problems in various countries, how to make the refining process of cyclohexanol more energy-saving and realize the environment-friendly and green production becomes a hot point of research at home and abroad.
The utility model adopts the energy-saving and consumption-reducing technology to fully utilize the heat of the cyclohexanol product coming out of the cyclohexanol rectifying tower, and reduces the steam energy consumption required by preheating the discharged cyclohexene of the bubble cap layer of the cyclohexanol separating tower, thereby not only having great significance for energy saving and consumption reduction, but also being beneficial to improving the economic benefit of enterprises and promoting the steady, rapid and continuous development of the enterprises.
Disclosure of Invention
The utility model aims to solve the problems in the background and provide an energy-saving system of a cyclohexanol separation tower and a cyclohexanol rectifying tower, wherein heat of cyclohexanol discharged from the cyclohexanol separation tower is absorbed by cyclohexene discharged from a bubble cap layer of the cyclohexanol separation tower, so that energy for heating cyclohexene fed into a hydration reactor is reduced, and meanwhile, the consumption of circulating cooling water for cooling the heat of cyclohexanol discharged from the cyclohexanol separation tower is reduced.
In order to achieve the above purpose, the present utility model adopts the following scheme:
the energy-saving system for the cyclohexanol separation tower and the cyclohexanol rectifying tower comprises a hydration reactor, a cyclohexanol separation tower, a cyclohexanol rectifying tower feed evaporator, a cyclohexanol rectifying tower feed spray separator and a cyclohexanol rectifying tower which are sequentially connected through pipelines; the cyclohexanol separating tower is provided with a bubble cap layer cyclohexene outlet and a bottom cyclohexanol outlet, and the bottom cyclohexanol outlet is connected with a cyclohexanol rectifying tower feed evaporator through a pipeline; the middle part of the cyclohexanol rectifying tower is provided with a cyclohexanol outlet, the bottom of the cyclohexanol rectifying tower is provided with a heavy component outlet, the cyclohexanol outlet in the middle part of the cyclohexanol rectifying tower is connected with a cyclohexanol 1# cooler through a pipeline, the outlet of the cyclohexanol 1# cooler is connected with the tube side of a cyclohexanol 2# cooler through a pipeline, the cyclohexene outlet of a bubble cap layer of a cyclohexanol separating tower is connected with the shell side inlet of the cyclohexanol 2# cooler, and the shell side outlet of the cyclohexanol 2# cooler is connected with the inlet of a hydration reactor.
Further, a gas phase outlet at the top of the cyclohexanol separation tower is connected with a cyclohexanol separation tower reflux tank, and the lower part of the cyclohexanol separation tower is connected with a cyclohexanol separation tower reboiler; the cyclohexanol knockout tower reflux tank is equipped with oil phase export and aqueous phase export, and the oil phase export links to each other with the backward flow mouth on cyclohexanol knockout tower upper portion through return conduit and the cyclohexanol knockout tower backwash pump of locating on the pipeline, and the branch is equipped with the extraction pipeline on the return conduit.
Further, a gas phase outlet at the top of the cyclohexanol rectifying tower is connected with a cyclohexanol rectifying tower reflux tank, and the lower part of the cyclohexanol rectifying tower is connected with a cyclohexanol rectifying tower reboiler; the cyclohexanol rectifying tower reflux tank is provided with an oil phase outlet and a water phase outlet, and the oil phase outlet is respectively connected with a reflux port at the upper part of the cyclohexanol rectifying tower and a reflux port at the middle part of the cyclohexanol separating tower through a pipeline and a cyclohexanol rectifying tower reflux pump arranged on the pipeline.
Further, a cyclohexanol separation tower cooler is arranged on the pipeline between the top gas phase outlet of the cyclohexanol separation tower and the reflux tank of the cyclohexanol separation tower.
Further, a cyclohexanol rectifying tower cooler is arranged on a pipeline between a top gas phase outlet of the cyclohexanol rectifying tower and a reflux tank of the cyclohexanol rectifying tower.
Further, a cyclohexanol separation tower kettle pump is arranged on a pipeline between a bottom cyclohexanol outlet of the cyclohexanol separation tower and a cyclohexanol rectifying tower feeding evaporator.
Further, a cold source inlet of the cyclohexanol 1# cooler is connected with a mixer, and a cyclohexanol discharge pump is arranged on a pipeline behind the cyclohexanol 1# cooler and the cyclohexanol 2# cooler.
Further, a heavy component outlet at the bottom of the cyclohexanol rectifying tower is provided with a heavy component extraction pipeline, and a cyclohexanol rectifying tower kettle pump is arranged on the heavy component extraction pipeline.
Further, a hydration reactor feed pump is arranged on a cyclohexene outlet pipeline of the bubble cap layer of the cyclohexanol separating tower.
The utility model can absorb the heat of the cyclohexanol discharged by the cyclohexene from the bubble cap layer of the cyclohexanol separating tower without adding large-scale equipment, thereby reducing the energy source for heating the cyclohexene fed into the hydration reactor and reducing the consumption of circulating cooling water for cooling the heat of the cyclohexanol discharged.
Drawings
Fig. 1 is a schematic structural view of the present utility model.
In the figure: 1. a cyclohexanol separation column, 2, a cyclohexanol separation column cooler, 3, a cyclohexanol separation column reflux drum, 4, a cyclohexanol separation column reflux pump, 5, a hydration reactor feed pump, 6, a cyclohexanol separation column reboiler, 7, a cyclohexanol separation column tank pump, 8, a cyclohexanol rectification column feed evaporator circulation pump, 9, a cyclohexanol rectification column feed evaporator, 10, a cyclohexanol rectification column feed spray separator, 11, a cyclohexanol 1# cooler, 12, a cyclohexanol discharge pump, 13, a cyclohexanol rectification column reboiler, 14, a cyclohexanol rectification column tank pump, 15, a cyclohexanol 2# cooler, 16, a mixer, 17, a cyclohexanol rectification column, 18, a cyclohexanol rectification column reflux pump, 19, a cyclohexanol rectification column reflux drum, 20, a cyclohexanol rectification column cooler, WC. cooling water (in) a wcr cooling water (in) a cch. High temperature condensed water (in) a LC. level gauge, TC. thermometer.
Detailed Description
The utility model is further described below with reference to the accompanying drawings.
Example 1
The energy-saving system of the cyclohexanol separation tower and the cyclohexanol rectifying tower is shown in figure 1, and comprises a hydration reactor (not shown in the figure), a cyclohexanol separation tower 1, a cyclohexanol rectifying tower feed evaporator 9, a cyclohexanol rectifying tower feed spray separator 10 and a cyclohexanol rectifying tower 17 which are connected in sequence through pipelines; the cyclohexanol separation tower 1 is provided with a bubble cap layer cyclohexene outlet and a bottom cyclohexanol outlet, and the bottom cyclohexanol outlet is connected with a cyclohexanol separation tower kettle pump 7 and a cyclohexanol rectifying tower feeding evaporator 9 which are arranged on the pipeline; the middle part of the cyclohexanol rectifying tower 17 is provided with a cyclohexanol outlet, the bottom is provided with a heavy component outlet, the cyclohexanol outlet in the middle part of the cyclohexanol rectifying tower 17 is connected with a cyclohexanol 1# cooler 11 through a pipeline, the outlet of the cyclohexanol 1# cooler 11 is connected with the tube side of a cyclohexanol discharge pump 12 arranged on the pipeline and a cyclohexanol 2# cooler 15, and the cyclohexene outlet of a cyclohexanol separating tower 1 bubble cap layer is connected with the shell side inlet of the cyclohexanol 2# cooler 15 through the pipeline and a hydration reactor feed pump 5 arranged on the pipeline.
The top gas phase outlet of the cyclohexanol knockout tower 1 is connected with a cyclohexanol knockout tower reflux tank 3, a cyclohexanol knockout tower cooler 2 is also arranged on a pipeline between the top gas phase outlet of the cyclohexanol knockout tower 1 and the cyclohexanol knockout tower reflux tank 3, the lower part of the cyclohexanol knockout tower 1 is connected with a cyclohexanol knockout tower reboiler 6, the cyclohexanol knockout tower reflux tank 3 is provided with an oil phase outlet and a water phase outlet, the oil phase outlet is connected with a reflux port on the upper part of the cyclohexanol knockout tower 1 through a reflux pipeline and a cyclohexanol knockout tower reflux pump 4 arranged on the pipeline, and a branch is arranged on the reflux pipeline.
The top gas phase outlet of the cyclohexanol rectifying tower 17 is connected with a cyclohexanol rectifying tower reflux tank 19, a cyclohexanol rectifying tower cooler 20 is further arranged on a pipeline between the top gas phase outlet of the cyclohexanol rectifying tower 17 and the cyclohexanol rectifying tower reflux tank 19, the lower part of the cyclohexanol rectifying tower 17 is connected with a cyclohexanol rectifying tower reboiler 13, the cyclohexanol rectifying tower reflux tank 19 is provided with an oil phase outlet and a water phase outlet, and the oil phase outlet is respectively connected with a reflux port of the upper part of the cyclohexanol rectifying tower 17 and a reflux port of the middle part of the cyclohexanol separating tower 1 through a pipeline and a cyclohexanol rectifying tower reflux pump 18 arranged on the pipeline.
The cold source inlet of the cyclohexanol 1# cooler 11 is connected with the mixer 16.
The heavy component outlet at the bottom of the cyclohexanol rectifying tower 17 is provided with a heavy component extraction pipeline, and the heavy component extraction pipeline is provided with a cyclohexanol rectifying tower kettle pump 14.
The cyclohexanol rectifying column feed evaporator 9 is provided with a cyclohexanol rectifying column feed evaporator circulation pump 8.
The actual working flow is as follows: the materials from the hydration reactor comprise water, cyclohexene, cyclohexanol and a small amount of hydration catalyst, the components enter the cyclohexanol separation tower 1 and are concentrated by a cyclohexanol separation tower reboiler 6, cyclohexene in a tower bubble cap layer is returned to the hydration reactor for continuous reaction by heat exchange with a cyclohexanol 2# cooler 15 through a hydration reactor feed pump 5, low boiling point substances on the tower top are condensed by the cyclohexanol separation tower cooler 2 and stored in a cyclohexanol separation tower reflux tank 3, a baffle plate in the cyclohexanol separation tower reflux tank 3 can separate water from oil components, a water bag at the lower part can discharge water, the oil components in the cyclohexanol separation tower reflux tank 3 are stable by controlling the tower top components by reflux in a part of the cyclohexanol separation tower reflux pump 4, and a part of the oil components are extracted. The material in the bottom of the cyclohexanol separating tower 1 is sent to a cyclohexanol rectifying tower feeding evaporator 9 through a cyclohexanol separating tower bottom pump 7, evaporation is carried out in the cyclohexanol rectifying tower feeding evaporator 9, and a cyclohexanol rectifying tower feeding evaporator circulating pump 8 is arranged on the cyclohexanol rectifying tower feeding evaporator 9, so that hydration catalyst is prevented from concentrating and blocking a pipeline, and periodical discharge is carried out. The cyclohexanol rectifying column feed spray separator 10 removes liquid droplets from the material evaporated from the cyclohexanol rectifying column feed evaporator 9, and then enters into the cyclohexanol rectifying column 17, the cyclohexanol rectifying column 17 is evaporated by the cyclohexanol rectifying column reboiler 13, the overhead low boiling substance containing cyclohexene and water is cooled by the cyclohexanol rectifying column cooler 20 and then stored in the cyclohexanol rectifying column reflux tank 19, and the components in the cyclohexanol rectifying column reflux tank 19 are reflux-controlled into the column by a portion of the cyclohexanol rectifying column reflux pump 18 to stabilize the overhead components, and a portion is returned into the cyclohexanol separating column 1. The heavy components in the bottom of the cyclohexanol rectifying tower 17 are discharged outwards periodically through a cyclohexanol rectifying tower bottom pump 14. The cyclohexanol is extracted from the middle section of the cyclohexanol rectifying tower 17 as steam, the refined cyclohexanol steam is condensed by a cyclohexanol 1# cooler 11, the circulation condensed water is mixed with high-temperature condensed water of the device by a mixer 16 to cool the cyclohexanol 1# cooler 11, the cooled cyclohexanol is stored in a tank at the lower part of the cyclohexanol 1# cooler 11, and then the cyclohexanol is extracted to a cyclohexanol 2# cooler 15 through a cyclohexanol discharge pump 12 to be cooled again and then sent to a cyclohexanol product storage tank.
Finally, it should be noted that: the above examples are provided for illustrating the technical solution of the present utility model and are not to be construed as limiting the present utility model, and it should be understood by those skilled in the art that any equivalent or obvious modification of the embodiments of the present utility model without changing the performance or use thereof without departing from the spirit of the present utility model is intended to be included in the scope of the present utility model as claimed.
Claims (9)
1. The energy-saving system for the cyclohexanol separation tower and the cyclohexanol rectifying tower is characterized by comprising a hydration reactor, a cyclohexanol separation tower, a cyclohexanol rectifying tower feed evaporator, a cyclohexanol rectifying tower feed spray separator and a cyclohexanol rectifying tower which are sequentially connected through pipelines; the cyclohexanol separating tower is provided with a bubble cap layer cyclohexene outlet and a bottom cyclohexanol outlet, and the bottom cyclohexanol outlet is connected with a cyclohexanol rectifying tower feed evaporator through a pipeline; the middle part of the cyclohexanol rectifying tower is provided with a cyclohexanol outlet, the bottom of the cyclohexanol rectifying tower is provided with a heavy component outlet, the cyclohexanol outlet in the middle part of the cyclohexanol rectifying tower is connected with a cyclohexanol 1# cooler through a pipeline, the outlet of the cyclohexanol 1# cooler is connected with the tube side of a cyclohexanol 2# cooler through a pipeline, the cyclohexene outlet of a bubble cap layer of a cyclohexanol separating tower is connected with the shell side inlet of the cyclohexanol 2# cooler, and the shell side outlet of the cyclohexanol 2# cooler is connected with the inlet of a hydration reactor.
2. The energy-saving system for the cyclohexanol separation tower and the cyclohexanol rectifying tower according to claim 1, wherein a top gas phase outlet of the cyclohexanol separation tower is connected with a cyclohexanol separation tower reflux tank, and a cyclohexanol separation tower reboiler is connected with the lower part of the cyclohexanol separation tower; the cyclohexanol knockout tower reflux tank is equipped with oil phase export and aqueous phase export, and the oil phase export links to each other with the backward flow mouth on cyclohexanol knockout tower upper portion through return conduit and the cyclohexanol knockout tower backwash pump of locating on the pipeline, and the branch is equipped with the extraction pipeline on the return conduit.
3. The energy-saving system for a cyclohexanol separation tower and a cyclohexanol rectifying tower according to claim 2, wherein a top gas phase outlet of the cyclohexanol rectifying tower is connected with a cyclohexanol rectifying tower reflux tank, and a cyclohexanol rectifying tower reboiler is connected with the lower part of the cyclohexanol rectifying tower; the cyclohexanol rectifying tower reflux tank is provided with an oil phase outlet and a water phase outlet, and the oil phase outlet is respectively connected with a reflux port at the upper part of the cyclohexanol rectifying tower and a reflux port at the middle part of the cyclohexanol separating tower through a pipeline and a cyclohexanol rectifying tower reflux pump arranged on the pipeline.
4. The energy-saving system for a cyclohexanol separation tower and a cyclohexanol rectifying tower according to claim 2, wherein a cyclohexanol separation tower cooler is further provided on a pipe between a top gas phase outlet of the cyclohexanol separation tower and a cyclohexanol separation tower reflux tank.
5. A cyclohexanol separator and cyclohexanol rectifying tower energy saving system according to claim 3, wherein a cyclohexanol rectifying tower cooler is further provided on the pipe between the top gas phase outlet of the cyclohexanol rectifying tower and the cyclohexanol rectifying tower reflux drum.
6. The energy-saving system for a cyclohexanol separation tower and a cyclohexanol rectifying tower according to claim 1, wherein a cyclohexanol separation tower kettle pump is arranged on a pipeline between a bottom cyclohexanol outlet of the cyclohexanol separation tower and a cyclohexanol rectifying tower feed evaporator.
7. The energy-saving system for the cyclohexanol separation tower and the cyclohexanol rectifying tower according to claim 1, wherein a cold source inlet of the cyclohexanol 1# cooler is connected with a mixer, and a cyclohexanol discharge pump is arranged on a pipeline behind the cyclohexanol 1# cooler and the cyclohexanol 2# cooler.
8. The energy-saving system for the cyclohexanol separation tower and the cyclohexanol rectifying tower according to claim 1, wherein a heavy component outlet at the bottom of the cyclohexanol rectifying tower is provided with a heavy component extraction pipeline, and the heavy component extraction pipeline is provided with a cyclohexanol rectifying tower kettle pump.
9. The energy-saving system for a cyclohexanol separation tower and a cyclohexanol rectifying tower according to claim 1, wherein a hydration reactor feed pump is arranged on a cyclohexene outlet pipe of a cyclohexanol separation tower bubble cap layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321574652.7U CN220090530U (en) | 2023-06-20 | 2023-06-20 | Cyclohexanol knockout tower and cyclohexanol rectifying column economizer system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321574652.7U CN220090530U (en) | 2023-06-20 | 2023-06-20 | Cyclohexanol knockout tower and cyclohexanol rectifying column economizer system |
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| Publication Number | Publication Date |
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| CN220090530U true CN220090530U (en) | 2023-11-28 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321574652.7U Active CN220090530U (en) | 2023-06-20 | 2023-06-20 | Cyclohexanol knockout tower and cyclohexanol rectifying column economizer system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220090530U (en) |
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2023
- 2023-06-20 CN CN202321574652.7U patent/CN220090530U/en active Active
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