CN219209016U

CN219209016U - KA oil device hydrogenation flash tank and dehydration tower economizer system

Info

Publication number: CN219209016U
Application number: CN202320800031.XU
Authority: CN
Inventors: 张乐; 高先明; 邹柯柯; 高庆福; 张磊磊; 孙维本; 姜阅民; 李森; 周高峰; 周丰雅; 王志军; 赵红伟; 刘跃旭; 于洋; 苏煜川; 赵岩; 李润翊; 董彦令; 郝丽娜; 代永豪
Original assignee: HENAN SHENMA NYLON CHEMICAL CO Ltd
Current assignee: HENAN SHENMA NYLON CHEMICAL CO Ltd
Priority date: 2023-04-12
Filing date: 2023-04-12
Publication date: 2023-06-20
Anticipated expiration: 2033-04-12

Abstract

The utility model discloses an energy-saving system for a hydrogenation flash tank and a dehydration tower of a KA oil device, which aims at the problems that the product oil phase from the hydrogenation flash tank has higher temperature and a certain latent heat and needs to consume a large amount of circulating cooling water to cool oil components when a hydrogenation reaction product of the KA oil device enters a dehydration tower reflux tank after being cooled by the hydrogenation flash tank and a subsequent condenser.

Description

KA oil device hydrogenation flash tank and dehydration tower economizer system

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 hydrogenation flash tank and a dehydration tower of a KA oil device.

Background

The manufacture of KA oil (cyclohexanone/cyclohexanol mixture) is an extremely important process in the nylon industry. The main manufacturing method of KA oil is cyclohexane oxidation method before 2010, and most enterprises mainly adopt benzene partial hydrogenation and hydration reaction method to prepare KA oil after that because of low conversion rate and poor selectivity and environmental damage caused by waste alkali generation, and because hydrogenation and hydration processes are continuous phases based on water phase, the method has obvious advantages in environmental protection, safety and cost compared with cyclohexane oxidation method. In the KA oil production device, the oil component from the hydrogenation reactor mainly comprises benzene/cyclohexene/cyclohexane, part of hydrogen and a small amount of ultrapure water, and the hydrogen in the oil component needs to be removed through a hydrogenation flash tank, and the ultrapure water in the oil component needs to be removed through a dehydration tower, so that the normal operation of the following working procedures is ensured. Since the product oil component exiting the hydrogenation flash tank has a relatively high temperature and a certain latent heat is underutilized, and a large amount of circulating cooling water is consumed to cool the oil component, a large amount of circulating cooling water is consumed. The oil components from the hydrogenation flash tank in the original process are cooled by a condenser and then enter a dehydration tower system, so that the heat energy is lost, and the consumption of circulating cooling water is greatly increased.

How to fully utilize the heat of the high Wen Youzu minutes discharged from the hydrogenation flash tank and reduce the consumption of circulating cooling water in the condensation process has important significance for energy conservation and consumption reduction.

Disclosure of Invention

The utility model aims to provide an energy-saving system of a hydrogenation flash tank and a dehydration tower of a KA oil device.

Based on the above purpose, the utility model adopts the following technical scheme:

the utility model provides a KA oil plant hydrogenation flash tank and dehydration tower economizer system, including hydrogenation flash tank, the dehydration tower, the reflux drum, first heat exchanger, the second heat exchanger, the third heat exchanger, hydrogenation flash tank's middle part is equipped with the oil phase export, the dehydration tower top is equipped with the light component export, the dehydration tower bottom is equipped with heavy component discharge pipeline and to the first reboiler of dehydration tower bottom heat supply, the reflux drum is equipped with the aqueous phase import, the aqueous phase export, oil phase import and oil phase export, still including the second reboiler of locating the dehydration tower bottom, second reboiler and parallelly connected setting of first reboiler, hydrogenation flash tank's oil phase export links to each other through pipeline and second reboiler's shell side import, the shell side export of second reboiler links to each other through pipeline and second heat exchanger's tube side import, the tube side export of second heat exchanger links to each other with the oil phase import of reflux drum, the light component export at dehydration top links to each other through pipeline and third heat exchanger's tube side import, the tube side export of third heat exchanger links to each other with the water phase import of reflux drum.

Further, the top of the hydrogenation flash tank is provided with a hydrogen discharge pipeline, the middle part of the hydrogenation flash tank is also provided with an oil phase recovery port, the first heat exchanger is arranged on the hydrogen discharge pipeline, and the oil phase entrained in the hydrogen cooled and recovered by the first heat exchanger returns to the hydrogenation flash tank through the oil phase recovery port.

Further, the oil phase outlet of the reflux tank is connected with the top of the dehydration tower through a pipeline and a reflux pump, so that the oil phase separated by the reflux tank is returned to the top of the dehydration tower through the reflux pump for rectification so as to remove the water in the oil phase.

Further, the top of the reflux tank is provided with an overflow outlet, and the overflow outlet is connected with the third heat exchanger through a pipeline, so that overflowed gas enters the reflux tank together with the light component of the dehydration tower after being cooled by the third heat exchanger.

Further, a tower bottom pump is arranged on the heavy component discharge pipeline.

The utility model can fully utilize the high-temperature energy of the oil phase at the outlet of the hydrogenation flash tank, improves the utilization efficiency of heat energy, reduces the consumption of the reboiler steam at the bottom of the dehydration tower, even reduces the consumption of circulating water cooling water for cooling the high-temperature oil component in the second heat exchanger, indirectly reduces the consumption of the circulating water cooling water of the whole device, and achieves the design requirement and the expected aim. The consumption of low-pressure steam in the tower bottom of the dehydration tower is reduced from 3 tons per hour to 2 tons per hour, the dehydration tower operates normally according to 8000 hours in one year, 8000 tons of low-pressure steam are saved per year, 160 ten thousand yuan per year is saved per ton of low-pressure steam calculated according to 200 yuan, the load of the cooler B is reduced, 5 ten thousand tons of circulating cooling water are saved per year, 4 ten thousand yuan per ton is calculated according to 0.8 yuan, and 164 ten thousand yuan per year can be saved in total.

Drawings

FIG. 1 is a schematic diagram of the structure of the present utility model;

in the figure: 1. the hydrogenation flash tank, 21, the first reboiler, 22, the second reboiler, 3, the dehydration tower, 4, the reflux drum, 51, the first heat exchanger, 52, the second heat exchanger, 53, the third heat exchanger, 6, the tower bottom pump, 7, the reflux pump, 8, the drainage pipeline.

Detailed Description

The following describes the technical scheme of the present utility model in further detail with reference to the accompanying drawings, but the scope of the present utility model is not limited thereto.

Example 1

The energy-saving system of the KA oil device hydrogenation flash tank and the dehydration tower is shown in figure 1, and comprises a hydrogenation flash tank 1, a dehydration tower 3, a reflux tank 4, a first heat exchanger 51, a second heat exchanger 52 and a third heat exchanger 53, wherein the top of the hydrogenation flash tank is provided with a hydrogen discharge pipeline, the middle part of the hydrogenation flash tank 1 is provided with an oil phase recovery port and an oil phase outlet, the first heat exchanger 51 is arranged on the hydrogen discharge pipeline, and oil phase carried in hydrogen cooled and recovered by the first heat exchanger 51 returns to the hydrogenation flash tank 1 through the oil phase recovery port by the pipeline; the top of the dehydration tower 3 is provided with a light component outlet, the bottom of the dehydration tower 3 is provided with a heavy component discharge pipeline and a first reboiler 21 for supplying heat to the bottom of the dehydration tower 3, and the heavy component discharge pipeline is provided with a tower kettle pump 6.

The reflux drum 4 is provided with a water phase inlet, a water phase outlet, an oil phase inlet and an oil phase outlet, and further comprises a second reboiler 22 arranged at the bottom of the dehydration tower 3, wherein the second reboiler 22 and the first reboiler 21 are arranged in parallel, the oil phase outlet of the hydrogenation flash drum 1 is connected with the shell side inlet of the second reboiler 22 through a pipeline, the shell side outlet of the second reboiler 22 is connected with the tube side inlet of the second heat exchanger 52 through a pipeline, the tube side outlet of the second heat exchanger 52 is connected with the oil phase inlet of the reflux drum 4, the light component outlet at the top of the dehydration tower 3 is connected with the tube side inlet of the third heat exchanger 53 through a pipeline, and the tube side outlet of the third heat exchanger 53 is connected with the water phase inlet of the reflux drum 4.

The oil phase outlet of the reflux tank 4 is connected with the top of the dehydration tower 3 through a pipeline and a reflux pump 7 so that the oil phase separated by the reflux tank 4 is returned to the top of the dehydration tower 3 through the reflux pump 7 for rectification to remove the water in the oil phase.

The top of the reflux tank 4 is provided with an overflow outlet which is connected with the third heat exchanger 53 through a pipeline so that overflowed gas enters the reflux tank 4 together with the light component of the dehydration tower 3 after being cooled by the third heat exchanger 53.

When the hydrogenation flash tank is used, the oil phase collected in the hydrogenation flash tank 1 flows out from the middle part, enters the second heat exchanger 52 for cooling after exchanging heat with the second reboiler 22, enters the water phase side in the reflux tank 4, oil-water separation occurs at the oil phase side, the separated oil phase enters the oil phase side, the separated water phase is stored in a water drum at the water phase side, the water drum is provided with a water phase outlet, the water phase outlet is connected with the drainage pipeline 8, and the water phase separated by the reflux tank 4 is discharged through the drainage pipeline 8. The oil phase enters the top of the dehydration tower 3 through a reflux pump 7 to be rectified to remove the water in the oil component, and the oil component with the water content reaching the standard is discharged from the tower kettle through a tower kettle pump 6.

The high-temperature oil phase in the hydrogenation flash tank 1 is sent to the second reboiler 22 through a pipeline through energy-saving transformation of the hydrogenation flash tank and the dehydration tower of the KA oil device, and the extracted high-temperature oil phase is used as part of heat source of the reboiler of the 3 tower kettles of the dehydration tower, so that the high-temperature oil phase out of the hydrogenation flash tank 1 is recycled secondarily, low-pressure steam unit consumption for production of the dehydration tower 3 is reduced, the heat energy utilization rate is improved, and the load of the second heat exchanger and the consumption of circulating cooling water are reduced. Through the adoption of the energy-saving technology and the optimization of technological measures, the energy consumption is effectively reduced, the energy saving is realized, and the enterprise cost is reduced.

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

1. The utility model provides a KA oil plant hydrogenation flash tank and dehydration tower economizer system, including hydrogenation flash tank, the dehydration tower, the reflux drum, first heat exchanger, the second heat exchanger, the third heat exchanger, the middle part of hydrogenation flash tank is equipped with the oil phase export, the dehydration tower top is equipped with the light component export, the dehydration tower bottom is equipped with heavy component discharge pipeline and to the first reboiler of dehydration tower bottom heat supply, the reflux drum is equipped with the aqueous phase import, the aqueous phase export, oil phase import and oil phase export, a serial communication port, still including locating the second reboiler of dehydration tower bottom, second reboiler and first reboiler parallelly connected setting, the oil phase export of hydrogenation flash tank links to each other through pipeline and the shell side import of second reboiler, the shell side export of second reboiler links to each other through pipeline and the tube side import of second heat exchanger, the tube side export of second heat exchanger links to each other with the oil phase import of reflux drum, the light component export at dehydration tower top links to each other through pipeline and the tube side import of third heat exchanger, the tube side export of third heat exchanger links to each other with the water phase import of reflux drum.

2. The energy-saving system for the hydrogenation flash tank and the dehydration tower of the KA oil device according to claim 1, wherein a hydrogen discharge pipeline is arranged at the top of the hydrogenation flash tank, an oil phase recovery port is further arranged at the middle part of the hydrogenation flash tank, the first heat exchanger is arranged on the hydrogen discharge pipeline, and the oil phase entrained in the hydrogen cooled and recovered by the first heat exchanger is returned to the hydrogenation flash tank through the oil phase recovery port by the pipeline.

3. The energy saving system of the KA oil device hydrogenation flash tank and the dehydration tower according to claim 1, wherein the oil phase outlet of the reflux tank is connected with the top of the dehydration tower through a pipeline and a reflux pump, so that the oil phase separated by the reflux tank is returned to the top of the dehydration tower through the reflux pump for rectification so as to remove water in the oil phase.

4. The energy-saving system for the hydrogenation flash tank and the dehydration tower of the KA oil device according to claim 1, wherein the top of the reflux tank is provided with an overflow port, and the overflow port is connected with the third heat exchanger through a pipeline so that overflowed gas enters the reflux tank together with light components of the dehydration tower after being cooled by the third heat exchanger.

5. The energy saving system for a hydrogenation flash tank and a dehydration tower of a KA oil device according to claim 1, wherein a tower bottom pump is arranged on the heavy component discharge pipeline.