CN213347782U - Ethylene glycol regenerating device - Google Patents

Abstract

The utility model relates to an ethylene glycol regenerating device, which comprises a regenerating tower, wherein the inner side of the regenerating tower is provided with a rich liquid side and a lean liquid side; the rich liquid heating system is connected with the rich liquid side of the regeneration tower; the rich liquid heating system comprises a reboiler connected with the regeneration tower; a desalination system connected to the lean liquid side of the regeneration tower; the cooling system is connected with the regeneration tower to cool the steam output by the regeneration tower and comprises a cooler connected with the regeneration tower and a reflux water tank connected with the cooler and the regeneration tower to collect the liquid cooled by the cooler and supply the liquid to reflux to the regeneration tower; the vacuum system is connected with the reflux water tank to carry out pressure transformation on the regeneration tower so as to adjust the boiling point of liquid in the regeneration tower; and the scale inhibitor input pipeline is connected with the rich liquid side of the regeneration tower so as to fill the scale inhibitor to the rich liquid side of the regeneration tower. The ethylene glycol regeneration device has the advantages of simple process, stable operation, energy conservation and environmental protection, and is favorable for slowing down the scale formation of the reboiler, reducing the medicament consumption caused by the cleaning of the reboiler and reducing the labor cost.

Description

Ethylene glycol regenerating device

Technical Field

The utility model relates to a glycol retrieves the field, and more specifically says, relates to a glycol regenerating unit.

Background

With the development of the marine natural gas development process, more and more underwater production systems are adopted for production, but the water-containing high-pressure low-temperature natural gas can easily form natural gas hydrate to freeze and block underwater structures. In order to inhibit the formation of the inhibitor, the hydrate inhibitor needs to be continuously injected into the underwater production system, the glycol is non-toxic, has a higher boiling point than methanol, has small evaporation loss, can be recycled by using a glycol regeneration device, and effectively reduces the operation cost. The ethylene glycol regeneration device is generally used for removing water in an ethylene glycol rich solution through a distillation principle to enable the ethylene glycol rich solution to become a barren solution, and aiming at the condition that offshore formation water contains much salt, the ethylene glycol regeneration device is also provided with a desalination unit for removing salt, and salt ions can form scale on the surface of a reboiler after long-term operation due to high regeneration temperature, so that the problems of low thermal efficiency and serious corrosion are caused.

Meanwhile, the reboiler mainly heats the rich solution in the system to over 125 ℃ to remove most of water in the ethylene glycol rich solution, so that the heat load of the reboiler is very large under the condition of large treatment capacity, and the offshore platform has a limited space, thereby bringing great difficulty to the design and model selection of the reboiler.

SUMMERY OF THE UTILITY MODEL

The to-be-solved technical problem of the utility model is to provide an improved ethylene glycol regenerating unit.

The utility model provides a technical scheme that its technical problem adopted is: a glycol regeneration device is constructed, comprising

The inner side of the regeneration tower is provided with a rich liquid side and a lean liquid side;

the rich liquid heating system is connected with the rich liquid side of the regeneration tower and is used for heating and dehydrating the rich liquid output by the regeneration tower; the rich liquid heating system comprises a reboiler connected to the regeneration column;

a desalination system connected to the lean liquid side of the regeneration tower for desalinating the lean liquid output from the regeneration tower;

the cooling system is connected with the regeneration tower to cool the steam output by the regeneration tower, and comprises a cooler connected with the regeneration tower and a reflux water tank connected with the cooler and the regeneration tower to collect the liquid cooled by the cooler and supply the liquid to reflux to the regeneration tower;

the vacuum system is connected with the reflux water tank to carry out pressure swing on the regeneration tower so as to adjust the boiling point of liquid in the regeneration tower;

an antiscalant input line connected to the rich liquid side of the regeneration column to fill antiscalant to the rich liquid side of the regeneration column.

Preferably, the rich liquid heating system further comprises a rich liquid output line connected to the reboiler and the rich liquid side of the regeneration tower, a first basket filter disposed on the rich liquid output line, a first centrifugal pump disposed on the rich liquid output line and between the first basket filter and the reboiler, and a lean liquid input line connected to the reboiler and the lean liquid side of the regeneration tower.

Preferably, the rich liquid output pipeline is connected with a pickling agent output pipeline;

and the lean liquid side input pipeline is connected with a pickling agent input pipeline.

Preferably, the desalination system comprises a lean liquid output line connected to the lean liquid side of the regeneration tower, a second centrifugal pump disposed on the lean liquid output line, a desalination device disposed at an end of the lean liquid output line remote from the lean liquid side, a second basket filter disposed on the lean liquid output line between the second centrifugal pump and the lean liquid side, and a rich liquid input line connecting the desalination device and the rich liquid side of the regeneration tower.

Preferably, the lean liquid output line is connected to the rich liquid output line;

the ethylene glycol regeneration device also comprises a standby component, wherein the standby component comprises a standby pipeline and a third basket filter arranged on the standby pipeline;

both ends of the standby pipeline are connected with the lean liquid output pipeline and the rich liquid output pipeline;

and the rich liquid output line is positioned on two opposite sides of the first basket filter, and/or the lean liquid output line is positioned on two opposite sides of the second basket filter, and/or the standby line is provided with isolation valves on two opposite sides of the third basket filter.

Preferably, the cooling system further comprises a vapor input line connected to the cooler and the regeneration tower, and a return line connected to the cooler and the return water tank;

the cooler is connected with an external cold source system.

Preferably, the cooling system further includes a liquid input line connected to the reflux water tank and the regeneration tower, and a third centrifugal pump provided on the liquid input line.

Preferably, a flow control valve is arranged on the liquid input pipeline.

Preferably, a closed-off system is further included in connection with the rich liquid side of the regeneration column.

Preferably, a pretreatment system connected with the rich liquid side of the regeneration tower is further included;

the scale inhibitor input pipeline is connected with the pretreatment system;

and a fourth centrifugal pump is arranged on the scale inhibitor input pipeline.

Implement the utility model discloses an ethylene glycol regenerating unit has following beneficial effect: this ethylene glycol regenerating unit is connected with vacuum system through the backward flow water pitcher with cooling system, can carry out the vary voltage and then the boiling point of adjustable liquid in the regenerator column to the regenerator column, changes reboiler temperature set point to change the heat load of reboiler, specifically, can step down this regenerator column, thereby reduce the temperature set point of reboiler, and then reduce the heat load of reboiler, reduce the salinity suction. In addition, by adding a scale inhibitor input pipeline on the rich liquid side of the regeneration tower, the generation of scales on the reboiler can be reduced by filling the scale inhibitor. The ethylene glycol regeneration device has the advantages of simple process, stable operation, energy conservation and environmental protection, and is favorable for slowing down the scale formation of the reboiler, reducing the medicament consumption caused by the cleaning of the reboiler and reducing the labor cost.

Drawings

The invention will be further explained with reference to the drawings and examples, wherein:

fig. 1 is a schematic diagram of an ethylene glycol regeneration device according to some embodiments of the present invention.

Detailed Description

In order to clearly understand the technical features, objects, and effects of the present invention, embodiments of the present invention will be described in detail with reference to the accompanying drawings.

Fig. 1 shows some preferred embodiments of the ethylene glycol regeneration device of the present invention. The ethylene glycol regeneration device can be used for recovering ethylene glycol. The ethylene glycol regeneration device has the advantages of simple process, stable operation, energy conservation and environmental protection, and is beneficial to slowing down the scale formation of the reboiler (H-1), reducing the medicament consumption caused by cleaning the reboiler (H-1) and reducing the labor cost.

As shown in fig. 1, in some embodiments, the ethylene glycol regeneration device may include a regeneration column (TW-1)10, a rich liquid heating system 20, a desalination system 30, a backup assembly 40, a cooling system 50, and a vacuum system 60. The regeneration column (TW-1)10 can be used for recovering and storing ethylene glycol. The rich liquid heating system 20 may be connected to the regeneration tower (TW-1)10, and may heat the rich liquid output from the regeneration tower (TW-1) 10. The desalination system 30 may be connected to the regeneration tower (TW-1)10, and may be used to desalinate the lean solution output from the regeneration tower (TW-1) 10. The backup assembly 40 can be coupled to the desalination system 30 and the rich liquid heating system 20 and can be used as a backup for the desalination system 30 and the rich liquid heating system 20. The cooling system 50 is connected to the regeneration tower (TW-1)10, and can be used for cooling the steam output from the regeneration tower (TW-1) 10. The vacuum system 60 is connectable to the cooling system 50 and is operable to vary the pressure of the regenerator column (TW-1)10, thereby adjusting the boiling point of the liquid in the regenerator column (TW-1)10, varying the temperature set point of the reboiler (H-1), thereby varying the heat duty of the reboiler (H-1), and in particular, to depressurize the regenerator column (TW-1), thereby lowering the temperature set point of the reboiler (H-1), thereby lowering the heat duty of the reboiler (H-1), and thereby reducing the salt draw.

Further, in some embodiments, the material of the regeneration column (TW-1)10 is 316LS duplex stainless steel, and a partition board can be arranged in the middle of the regeneration column (TW-1)10, and the partition board can divide the inner side of the regeneration column (TW-1)10 into a rich liquid side 11 and a lean liquid side 12. The rich side 11 may be filled with rich liquid and may also have a skimmer to remove small amounts of heavy hydrocarbons from the system. The lean side 12 is available for lean liquor charging. The upper part of the regeneration tower (TW-1)10 can be provided with a tray and a reflux water uniform distributor. The tray can be used for separating a gas-liquid mixture. The regeneration column (TW-1)10 can be designed as a vacuum vessel which can satisfy the external pressure resistance of 0.1MPa, and the pressure of the regeneration column (TW-1)10 can be maintained at a vacuum of 0.2bara by the vacuum system 60 in operation. It should be noted that the regeneration column (TW-1)10 was checked for external pressure resistance and stability. In some embodiments, an absolute pressure transmitter and an absolute pressure gauge may be mounted on the regeneration column (TW-1) 10.

Further, in some embodiments, the rich liquid heating system 20 may be connected to the rich liquid side 11, which may heat and dehydrate the rich liquid output from the regeneration tower (TW-1) 10. In some embodiments, the rich liquid heating system may include a rich liquid outlet line 21, a first centrifugal pump (P-2)22, a reboiler (H-1)23, a heat source device 24, a first basket filter (F-3)25, and a lean side inlet line 26. The rich liquid output line 21 has one end connected to the rich liquid side 11 of the regeneration column (TW-1)10 and the other end connected to the reboiler (H-1)23, and is configured to communicate the regeneration column (TW-1)10 with the reboiler (H-1)23, and the rich liquid output from the rich liquid side 11 can flow to the reboiler (H-1)23 through the rich liquid output line 21, and be heated and dehydrated by the reboiler (H-1) 23. The first centrifugal pump (P-2)22 may be disposed on the rich liquid output line 21, and may be located between the regeneration column (TW-1)10 and the reboiler (H-1)23, which may pump out the rich liquid in the rich liquid side 11 of the regeneration column (TW-1) 10. The reboiler (H-1)23 may be disposed at one end of the rich liquid output line 21, and may be connected to the regeneration column (TW-1)10 through the rich liquid output line 21, and may be used to heat and dehydrate the rich liquid delivered from the rich liquid output line 21. The temperature set point of the reboiler (H-1)23 can be adjusted in accordance with the boiling point of ethylene glycol in the regeneration column (TW-1)10, that is, when the boiling point of ethylene glycol in the regeneration column (TW-1)10 is lowered, the temperature set point of the reboiler (H-1)23 can be lowered. The heat source device 24 can be connected to the reboiler (H-1)23, and can supply a heat source to the reboiler (H-1) 23. The first basket filter (F-3)25 may be disposed on the rich liquid output line 21, which may be located between the first centrifugal pump (P-2)22 and the regeneration tower (TW-1) 10. The lean liquid side input line 26 may have one end connected to the reboiler (H-1) and the other end connected to the lean liquid side 12 of the regeneration column (TW-1)10, and may input the lean liquid output from the reboiler (H-1)23 to the regeneration column (TW-1) 10.

In some embodiments, isolation valves V-5, V-8 may also be provided on the rich liquid outlet line 21. The two isolation valves V-5, V-8 are respectively positioned at two opposite sides of the first basket filter (F-3). It will be appreciated that in other embodiments, the isolation valves V-5, V-8 may be omitted. The rich liquid outlet line 21 may further include a level control valve LV-3, and the level control valve LV-3 may be located between the reboiler (H-1)23 and the first centrifugal pump (P-2)22, and may be used to control the liquid level of the rich liquid side 11 of the regeneration tower (TW-1) 10. In some embodiments, the level control valve LV-3 may be connected to the level transmitter L-3. In some embodiments, an isolation valve V-13 may be disposed on the lean liquid side input line 26, and the isolation valve V-13 is opened to allow lean liquid to be input to the lean liquid side of the regeneration column (TW-1) 10.

In some embodiments, the reboiler (H-1)23 may be a spiral plate heat exchanger. The inlet and outlet of the reboiler (H-1)23 can be provided with a differential pressure gauge which can be used for judging the scaling condition of the reboiler (H-1). In some embodiments, the outlet of the reboiler (H-1)23 may be sized larger than the inlet line to facilitate volume expansion after water evaporation.

In some embodiments, the heat source device 24 can be a hot kerosene system that can provide a heat source for the reboiler (H-1) 23. The outlet of the heat source device 24 may be provided with a temperature regulating valve TV-1, and the temperature regulating valve TV-1 may be used to control the heating temperature of the ethylene glycol rich. Of course, it is understood that in other embodiments, the heat source device 24 is not limited to a hot kerosene system, and in some embodiments, the heat source device 24 may be an electromagnetic heating device or other electrical heating device.

Further, in some embodiments, the rich liquor heating system 20 may also include a pickling agent output line 27 and a pickling agent input line 28. The acid wash outlet line 27 can be disposed on the rich liquid input line 21, can be located at the end of the rich liquid input line 21 connected to the reboiler (H-1)23, and can be in communication with the rich liquid input line 21, and can be disposed proximate to the inlet of the reboiler (H-1) 23. The acid washing agent outlet line 27 may be externally connected to an acid washing agent storage device for recovering the acid washing agent after the acid washing by the reboiler (H-1)23, and one end of the acid washing agent inlet line 28 may be externally connected to an acid washing agent storage device for introducing the acid washing agent into the reboiler (H-1) 23. The acid-washing agent input line 28 may be provided on the lean solution-side input line 26, and may be provided near the outlet of the reboiler (H-1)23, which communicates with the lean solution-side input line 26, and which can inject the acid-washing agent into the reboiler (H-1) 23. The inside of the reboiler (H-1)23 is cleaned by circulating the pickling agent through the pickling agent input line 28 and the pickling agent output line 27. In some embodiments, isolation valves V-12, V11 are provided on both the pickle outlet line 27 and the pickle inlet line 28.

When the reboiler (H-1)23 requires the acid cleaning, the flow switching is performed to close the isolation valves V-5, V-8 and V-13, the flow is switched to the acid cleaning flow, ethylene glycol in the reboiler (H-1)23 is evacuated, an acid cleaning agent is supplied to the reboiler (H-1)23 through the acid cleaning agent supply line 27 and the acid cleaning agent supply line 28, and the reboiler (H-1)23 is cyclically immersed in the acid cleaning agent, whereby the scale in the reboiler (H-1)23 can be removed.

Further, in some embodiments, the desalination system 30 can include a lean liquid outlet line 31, a second centrifugal pump (P-1)32, a desalination device 33, a second basket filter (F-1)34, and a rich liquid inlet line 35. The lean liquid output line 31 may be connected to the lean liquid side 12 of the regeneration tower (TW-1)10, and specifically, may have one end connected to the lean liquid side 12 of the regeneration tower (TW-1)10 and the other end connected to the desalination device 33, and the lean liquid output line 31 may input the lean liquid output from the lean liquid side 12 of the regeneration tower (TW-1)10 to the desalination device 33 for desalination. In some embodiments, the lean liquid output line 31 may be connected to the rich liquid output line 21, and the second centrifugal pump (P-1)32 may be disposed on the lean liquid output line 31 between the regeneration tower (TW-1)10 and the basket filter 34, which may be used to pump out the lean liquid of the regeneration tower (TW-1) 10. The desalination device 33 may be located at an end of the lean liquid output line 31 remote from the lean liquid side 12, which may be used to desalinate lean liquid. In some embodiments, the desalination device 33 can be a conventional device. The second basket filter (F-1)34 may be disposed on the lean liquid output line 31 between the second centrifugal pump (P-1)32 and the lean liquid side 12, and may filter the lean liquid output from the lean liquid side 12. The rich liquid input line 35 may be connected at one end to the desalination device 33 and at the other end to the rich side 11 of the regeneration column (TW-1) 10. The rich solution desalted by the desalting unit 33 can be inputted to the rich solution side 11 of the regeneration tower (TW-1)10 through the rich solution input line 35.

Further, in some embodiments, isolation valves V-3, V-6 may be provided on the lean output line 31; the two isolation valves V-3, V-6 are provided, and the two isolation valves V-3, V-6 are respectively provided on two opposite sides of the second basket filter (F-1) 34. It will be appreciated that in other embodiments, the isolation valves V-3, V-6 may be omitted. In some embodiments, a level control valve LV-2 may be disposed at the outlet of the second centrifugal pump (P-1)32, and the level control valve LV-2 may be used to adjust the liquid level of the lean side of the regeneration column (TW-1) 10. In some embodiments, the level control valve LV-2 may be connected to the level transmitter L-2.

In some embodiments, because the glycol solution is at a high temperature, the first centrifugal pump (P-2)22 and the second centrifugal pump (P-1)32 are connected to a mechanical seal cooling device, which may be an air cooling device or a water cooling device.

Further, in some embodiments, the backup assembly 40 may also include a backup line 41 and a third basket filter (F-2) 42. Both ends of the spare line 41 are connected to the lean liquid output line 31 and the rich liquid output line 21, respectively. Specifically, in some embodiments, two ends of the spare line 41 may be respectively provided with a three-way valve, and the three-way valve may be respectively connected with the lean liquid output line 31 and the rich liquid output line 21 through connecting lines. In some embodiments, isolation valves V-4, V-7 may be provided on this backup line 41. The two isolation valves V-4, V-7 are provided, and the two isolation valves V-4, V-7 are respectively provided on two opposite sides of the third basket filter (F-2) 42. In some embodiments, the input of the backup line 41 may be provided with isolation valves V-1, V-2; the isolation valve V-1 may be located between the spare line 41 and the lean liquid output line 31; the isolation valve V-2 may be disposed between the backup line 41 and the rich liquid output line 21. In some embodiments, the output of the backup line 41 may be provided with isolation valves V-9, V-10; the isolation valves V-9, V-10 may be two, wherein the isolation valve V-9 may be located between the standby line 41 and the lean liquid output line 31, and the isolation valve V-10 may be located between the standby line 41 and the rich liquid output line 21. It will be appreciated that in other embodiments, the backup assembly 40 may be omitted.

In some embodiments, the inlets of the first centrifugal pump (P-2)21 and the second centrifugal pump (P-1)22 may both be connected with basket filters. The first basket filter (F-3)25, the second basket filter (F-1)34 are main filters, the third basket filter (F-2)42 is a spare filter, and the system can be stopped when the first basket filter (F-3)25 or the second basket filter (F-1)34 is blocked and cleaned through outflow switching, so that the continuity of the system can be improved.

Further, in some embodiments, the cooling system 50 may be connected to a vapor outlet provided at the top of the regeneration tower (TW-1) 10. The cooling system 50 may include a steam input line 51, a cooler (WC-1)52, a return water tank (D-1)53, and a return line 54.

The steam input line 51 may be connected at one end to the regeneration column (TW-1)10 and at the other end to the cooler (WC-1) 52. The steam input line 51 may be used to output the steam output from the regeneration column (TW-1)10 to the cooler (WC-1) 52.

In some embodiments, the cooler (WC-1)52 may be connected to the regeneration column (TW-1)10 via a steam input line 51. The cooler (WC-1)52 may be a plate cooler (WC-1) whose hot end, through which the water vapor of the regeneration column (TW-1)10 can enter the interior of the cooler (WC-1), may be connected to the overhead vapor outlet of the regeneration column (TW-1) 10. In some embodiments, the hot end outlet of the cooler (WC-1)52 may be provided with a differential pressure gauge, which may be used to determine the operation of the cooler (WC-1). The cooler (WC-1)52 can be connected to an external heat sink system. Specifically, in some embodiments, the cold end of the chiller (WC-1)52 may be connected to an external cold sink system. The external cold source system can be a seawater system. The vapor entering the cooler (WC-1)52 can be cooled by the seawater at the cold end and then changed into liquid water to enter the return water tank (D-1) 53. In some embodiments, the hot end outlet of the cooler (WC-1)52 may be provided with a temperature control valve TV-2.

In some embodiments, the return water tank (D-1)53 may be connected to the cooler (WC-1)52 and the regeneration column (TW-1)10, and may be used to collect the liquid cooled by the cooler (WC-1)52 and provide for the liquid to return to the regeneration column (TW-1). Specifically, in some embodiments, the return water tank (D-1)53 may be connected to the cooler (WC-1)52 via a return line 54. The inlet on the return water tank (D-1)53 may be connected to the cold end of the cooler (WC-1)52 via a return line 54, and its outlet may be connected to the regeneration column (TW-1) 10. In some embodiments, the top of the return water tank (D-1)53 may be connected to the vacuum system 60. An absolute pressure meter and an absolute pressure transmitter can be arranged on the backflow water tank (D-1)53, the whole regeneration device can be changed into negative pressure through the vacuum system 60, and it should be noted that the backflow water tank (D-1)53 needs to be checked for external pressure resistance and stability, and all instruments used for the regeneration device need to work under the negative pressure, including but not limited to pressure, temperature, liquid level transmitters and field instruments.

In some embodiments, the return line 54 may be disposed between the cooler (WC-1)52 and the return water tank (D-1)53, and may be connected to the cooler (WC-1)52 at one end and the return water tank (D-1)53 at the other end.

In some embodiments, the cooling system 50 may also include a liquid input line 55 and a third centrifugal pump (P-3) 56. The liquid input line 55 may have one end connected to the reflux water tank (D-1)53 and the other end connected to the regeneration column (TW-1)10, which may reflux the liquid of the reflux water tank (D-1)53 to the regeneration column (TW-1) 10. The third centrifugal pump (P-3)56 may be disposed on the liquid input line 55, which may be used to pump the liquid of the return water tank (D-1)53 to the liquid input line 55. The liquid water cooled by the cold end of the cooler (WC-1)51 is introduced into a reflux water tank (D-1)53, and the refluxed liquid is pumped out to the liquid input line 55 by a third centrifugal pump (P-3)56, and is input into the regeneration column (TW-1)10 from the top of the regeneration column (TW-1)10 through the liquid input line 55. The liquid inlet line 55 may be connected to a process water treatment system via a connecting line. The liquid inlet line 55 may be provided with a flow control valve FV-1 adjacent the third centrifugal pump (P-3) 56. The pipeline connecting the liquid input pipeline 55 and the production water treatment system can be provided with a liquid level control valve LV-4, and the liquid level control valve LV-4 can be connected with the liquid level transmitter L-4.

Further, in some embodiments, the vacuum system 60 may be connected to the reflux water tank (D-1)53, which may vary the pressure of the regeneration column (TW-1)10, thereby adjusting the boiling point of the liquid in the regeneration column (TW-1) 10. Specifically, the boiling point of the regeneration column (TW-1)10 is reduced from normal pressure to 0.2bara, the boiling point of water is reduced from 100 ℃ which is normal pressure to 60 ℃, the temperature set point of the reboiler (H-1) is reduced from about 125 ℃ to 85 ℃, the heat load of the reboiler (H-1) is reduced, the temperature of the reboiler (H-1) is reduced, and the salt separation is reduced.

Further, in some embodiments, the ethylene glycol regeneration device may also include a pretreatment system 70. The pretreatment system 70 may be connected to the rich liquid side 11 of the regeneration column (TW-1)10, which may pretreat the rich liquid fed into the regeneration column (TW-1) 10. In some embodiments, the pre-treatment system 70 may be a conventional system.

The treated rich ethylene glycol solution from the pretreatment system 70 may enter the rich side 11 of the regeneration column (TW-1)10, then the rich liquid is output through the rich liquid output pipeline 21 and filtered by the first basket filter (F-3)25, the filtered rich liquid is pumped into the reboiler (H-1)23 through the first centrifugal pump (P-2)22 to be heated to 85 ℃, the boiling point of water is reduced to 60 ℃ under vacuum, after the temperature is raised by a reboiler (H-1)23, most of the water in the rich solution is evaporated to obtain 20 wt% lean solution, which enters the lean solution side 12 of the regeneration tower (TW-1)10 through the lean solution side input line 26, and the water vapor can reversely contact with the reflux water equilizer through a tray in the regeneration tower (TW-1)10 and carry out window heat transfer, thereby reducing the loss of ethylene glycol.

Further, in some embodiments, the scale inhibitor input line 80 may be connected to the pretreatment system 70. Specifically, in some embodiments, one end of the antiscalant input line 80 may be connected to the antiscalant storage device, and the other end may be connected to a line connecting the pretreatment system and the rich liquid side 11. The antisludging agent input pipeline 80 can be provided with a fourth centrifugal pump (P-4)81, the fourth centrifugal pump (P-4)81 can be used for pumping the antisludging agent into the rich liquid side 11 of the regeneration tower (TW-1)10, and then the generation of the dirt at the reboiler (H-1) can be reduced by filling the antisludging agent. In some embodiments, a flow control valve FV-2 may be disposed in the antiscalant inlet line 80. In some embodiments, the antiscalant may be a conventional antiscalant, but it may also be a weak acid that inhibits fouling by lowering the PH of reboiler 23.

Further, in some embodiments, the glycol regeneration device may also include a closed-circuit system 90. The closed drain system 90 may be connected to the rich side 11 of the regeneration column (TW-1)10, and in particular, in some embodiments, may be connected to the rich side 11 of the regeneration column (TW-1)10 by providing a drain line. A liquid level control valve LV-1 can be arranged on the pipeline, and the liquid level control valve LV-1 can be connected with the liquid level transmitter L-1. The rich side 11 is skimmed of a small amount of heavy hydrocarbons and is discharged to a closed drain system through level control valve LV-1.

As further shown in fig. 1, when the ethylene glycol regeneration apparatus is in operation, the rich ethylene glycol solution from the pretreatment system 70 can be introduced into the regeneration tower (TW-1)10, and the rich ethylene glycol solution is skimmed off a small amount of heavy hydrocarbons on the rich solution side 11 of the regeneration tower (TW-1)10, and then discharged to the closed discharge system through the discharge line by opening the level control valve LV-1. The isolation valves V-5, V-8, V-13 are opened, the ethylene glycol rich solution is outputted from the bottom rich solution output line 21 of the rich solution side 11 of the regeneration tower (TW-1)10 to the first basket filter (F-3)25, filtered by the first basket filter (F-3)25, boosted by the first centrifugal pump (P-2)22, and then sent to the reboiler (H-1)23 for temperature rise, wherein the temperature set point of the reboiler (H-1) can be 85 ℃ (the specific temperature set point can be adjusted according to actual working conditions). The rich ethylene glycol solution can enter from the cold end of the reboiler (H-1)23, the reboiler (H-1)23 can provide a heat source for the reboiler from a hot kerosene system, and the hot kerosene outlet can regulate the heating temperature through the temperature regulating valve TV-1. The ethylene glycol solution and water vapor heated and outputted by the reboiler (H-1)23 may be inputted to the lean liquid side 12 of the regeneration column (TW-1)10 through the lean liquid side input line 26. The isolation valve V-3 and the isolation valve V-6 are opened, and the glycol lean solution can be gathered at the lean solution side 12 of the regeneration tower (TW-1)10 and output to the second basket filter (F-1)34 through the lean solution output line 31, filtered by the second basket filter (F-1)34 and pumped into the desalination device 33 through the second centrifugal pump (P-1) 32. The flow regulating valve FV-1 is opened, the vapor in the regeneration tower (TW-1)10 can ascend to the top of the regeneration tower (TW-1)10, and contact with the reflux water at the tray in the reverse direction, transfer heat by mass, and then output to the cooler (WC-1)52 through the vapor input line 51 for cooling, and the cooled liquid becomes liquid and enters the reflux water tank (D-1)53 through the reflux line 54, and the reflux liquid is sent to the regeneration tower (TW-1)10 through the bottom of the reflux water tank (D-1) through the third centrifugal pump (P-3)56, the liquid input line 55, and the flow regulating valve FV-1, wherein the amount of water entering the production water system can be controlled by the level control valve LV-4 in the reflux water tank (D-1) 53. The top of the return water tank (D-1)53 may be connected to a vacuum system 60, and the entire regeneration apparatus is made negative by the vacuum system 60.

It is to be understood that the foregoing examples merely represent preferred embodiments of the present invention, and that the description thereof is more specific and detailed, but not intended to limit the scope of the invention; it should be noted that, for those skilled in the art, the above technical features can be freely combined, and several modifications and improvements can be made without departing from the concept of the present invention, which all belong to the protection scope of the present invention; therefore, all changes and modifications that come within the meaning and range of equivalency of the claims are to be embraced within their scope.

Claims (10)

1. The ethylene glycol regeneration device is characterized by comprising

A regeneration tower (10) provided with a rich liquid side (11) and a lean liquid side (12) on the inner side;

a rich liquid heating system (20) connected with the rich liquid side (11) of the regeneration tower (10) for heating and dehydrating the rich liquid output by the regeneration tower (10); the rich liquid heating system (20) comprises a reboiler (23) connected to the regeneration column (10);

a desalination system (30) connected to the lean liquid side (12) of the regeneration tower (10) for desalinating the lean liquid output from the regeneration tower (10);

the cooling system (50) is connected with the regeneration tower (10) to cool the steam output by the regeneration tower (10), and comprises a cooler (52) connected with the regeneration tower (10), and a reflux water tank (53) which is connected with the cooler (52) and the regeneration tower (10) to collect the liquid cooled by the cooler (52) and supply the liquid to reflux to the regeneration tower (10);

a vacuum system (60) connected to the reflux water tank (53) for varying the pressure of the regeneration column (10) to adjust the boiling point of the liquid in the regeneration column (10);

an antiscalant input line (80) connected to the rich liquid side (11) of the regeneration column (10) for filling an antiscalant to the rich liquid side (11) of the regeneration column (10).

2. Ethylene glycol regeneration device according to claim 1, characterized in that the rich liquid heating system (20) further comprises a rich liquid outlet line (21) connected to the reboiler (23) and the rich side (11) of the regeneration column (10), a first basket filter (25) arranged on the rich liquid outlet line (21), a first centrifugal pump (22) arranged on the rich liquid outlet line (21) between the first basket filter (25) and the reboiler (23), and a lean liquid side inlet line (26) connected to the reboiler (23) and the lean side (12) of the regeneration column (10).

3. The ethylene glycol regeneration apparatus according to claim 2, wherein a pickling agent outlet line (27) is connected to the rich liquid outlet line (21);

the lean liquid side input pipeline (26) is connected with a pickling agent input pipeline (28).

4. Ethylene glycol regeneration device according to claim 3, wherein the desalination system (30) comprises a lean liquid output line (31) connected to the lean liquid side (12) of the regeneration column (10), a second centrifugal pump (32) arranged on the lean liquid output line (31), a desalination device (33) arranged at an end of the lean liquid output line (31) remote from the lean liquid side (12), a second basket filter (34) arranged on the lean liquid output line (31) and located between the second centrifugal pump (32) and the lean liquid side (12), and a rich liquid input line (35) connecting the desalination device (33) and the rich liquid side (11) of the regeneration column (10).

5. Ethylene glycol regeneration device according to claim 4, characterized in that the lean liquid outlet line (31) is connected to the rich liquid outlet line (21);

the ethylene glycol regeneration device further comprises a standby assembly (40), wherein the standby assembly (40) comprises a standby pipeline (41), and a third basket filter (42) arranged on the standby pipeline (41);

both ends of the spare pipeline (41) are respectively connected with the lean liquid output pipeline (31) and the rich liquid output pipeline (21);

the rich liquid output line (21) is positioned on two opposite sides of the first basket filter (25), the lean liquid output line (31) is positioned on two opposite sides of the second basket filter (34), and/or the spare line (41) is provided with an isolation valve on two opposite sides of the third basket filter (42).

6. Ethylene glycol regeneration device according to claim 1, wherein the cooling system (50) further comprises a steam input line (51) connected to the cooler (52) and the regeneration column (10), and a return line (54) connected to the cooler (52) and the return water tank (53);

the cooler (52) is connected to an external cold source system.

7. Ethylene glycol regeneration device according to claim 6, characterized in that the cooling system (50) further comprises a liquid input line (55) connected to the return water tank (53) and the regeneration tower (10), and a third centrifugal pump (56) arranged on the liquid input line (55).

8. Ethylene glycol regeneration device according to claim 7, characterized in that a flow control valve is provided on the liquid input line (55).

9. The ethylene glycol regeneration device according to claim 1, further comprising a closed drain system (90) connected to the rich liquid side (11) of the regeneration column (10).

10. The ethylene glycol regeneration device according to claim 1, further comprising a pre-treatment system (70) connected to the rich liquid side (11) of the regeneration column (10);

the scale inhibitor input line (80) is connected with the pretreatment system (70);

and a fourth centrifugal pump (81) is arranged on the scale inhibitor input pipeline (80).

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