CN213446987U - Solvent recovery system of supercritical solvent deasphalting process unit - Google Patents
Solvent recovery system of supercritical solvent deasphalting process unit Download PDFInfo
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- CN213446987U CN213446987U CN202022162467.XU CN202022162467U CN213446987U CN 213446987 U CN213446987 U CN 213446987U CN 202022162467 U CN202022162467 U CN 202022162467U CN 213446987 U CN213446987 U CN 213446987U
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Abstract
The utility model relates to a solvent recovery system of supercritical solvent deasphalting process units, the deasphalting oil-solvent feed pipeline of the solvent recovery system enters a deasphalting oil separation tower after passing through a first deasphalting oil-solvent feed preheater and a second deasphalting oil-solvent feed preheater, a solvent outlet pipeline at the top of the deasphalting oil separation tower is connected with a circulating solvent loop, a residual solvent-deasphalting oil mixed solution outlet pipeline at the bottom of the deasphalting oil separation tower is connected with a deasphalting oil flash tank, a solvent outlet at the top of the deasphalting oil flash tank is connected with a low-pressure solvent circulating pipeline, a residual solvent-deasphalting oil mixed solution outlet pipeline at the bottom of the deasphalting oil flash tank is connected with the deasphalting oil flash tank through a preheater, a solvent outlet pipeline at the top of the deasphalting oil flash tank is connected with a low-pressure solvent circulating pipeline, an deasphalting oil product outlet pipeline, the deasphalted oil product outlet pipeline is connected with a deasphalted oil product pump. The utility model discloses effectively realize reducing the energy consumption, improve the purpose of system's benefit.
Description
Technical Field
The utility model belongs to the technical field of the supercritical solvent takes off pitch, especially a solvent recovery system of supercritical solvent takes off pitch process units.
Background
The supercritical solvent deasphalting process is a residual oil extraction process for separating residual oil into high-value deasphalted oil and low-value deasphalted asphalt. It features wide raw material application range and can be used to prepare catalytic cracking and hydrocracking raw materials and various asphalt products. The technology is mature, the flow and the equipment are simple, and the investment and the operation cost are low.
In a supercritical solvent deasphalting plant, the recovery of the solvent is a critical process for the plant. The recycling mode has important influence on the energy-saving effect of the whole device. The existing solvent recovery system has high energy consumption, and a technical scheme for further reducing the energy consumption and the cost needs to be provided.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome prior art's not enough, provide a solvent recovery system of supercritical solvent deasphalting process units, energy-conserving effect is further improved.
The utility model provides a its technical problem realize through following technical scheme:
a solvent recovery system of a supercritical solvent deasphalting process unit is characterized in that: the system comprises a first deasphalted oil-solvent feeding preheater, a second deasphalted oil-solvent feeding preheater, a deasphalted oil separation tower, a deasphalted oil flash tank, a stripper preheater, a deasphalted oil stripper and a deasphalted oil product pump, wherein a deasphalted oil-solvent feeding pipeline enters the deasphalted oil separation tower through the first deasphalted oil-solvent feeding preheater and the second deasphalted oil-solvent feeding preheater, a solvent outlet pipeline at the top of the deasphalted oil separation tower is connected with a circulating solvent loop, a residual solvent-deasphalted oil mixed solution outlet pipeline at the bottom of the deasphalted oil separation tower is connected with the deasphalted oil flash tank, a solvent outlet at the top of the deasphalted oil flash tank is connected with a low-pressure solvent circulating pipeline, a residual solvent-deasphalted oil mixed solution outlet pipeline at the bottom of the deasphalted oil flash tank is connected with the deasphalted oil flash tank through the preheater, the solvent outlet pipeline at the top of the deasphalted oil stripping tower is connected with a low-pressure solvent circulating pipeline, the deasphalted oil product outlet pipeline is arranged at the bottom of the deasphalted oil stripping tower, and the deasphalted oil product outlet pipeline is connected with a deasphalted oil product pump.
And a solvent outlet pipeline at the top of the deasphalted oil separation tower is connected with a first deasphalted oil-solvent feeding preheater and exchanges heat with the deasphalted oil-solvent feeding pipeline.
And the second deasphalted oil-solvent feeding preheater is connected with a heat transfer oil heat exchange pipeline.
And a first flow valve is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil separation tower, and the first flow valve is in control connection with a first tower bottom liquid level sensor in the deasphalted oil separation tower.
And a second flow valve is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil flash tank, and the second flow valve is in control connection with a second tower bottom liquid level sensor in the deasphalted oil flash tank.
And a third flow valve is arranged on the deasphalted oil product outlet pipeline, and the third flow valve is controlled in cascade by a third tower bottom liquid level sensor of the deasphalted oil stripping tower and a flow sensor behind a pump.
The utility model discloses an advantage and beneficial effect do:
1. the utility model discloses a solvent recovery system of supercritical solvent deasphalting process units, deasphalting oil knockout tower top solvent outlet pipe way connect first deasphalting oil-solvent feeding pre-heater, deasphalting oil-solvent feeding accessible and the top material heat transfer of deasphalting oil knockout tower carry out certain heat recovery, and the feeding preheats all the other heats and is provided by the conduction oil through second deasphalting oil-solvent feeding pre-heater.
2. The utility model discloses a solvent recovery system of supercritical solvent deasphalting process units, deasphalting oil-solvent feeding mainly realize dividing in the deasphalting oil knockout tower, under supercritical state, 95 wt% solvent separation, this circulation solvent gets into solvent circulation loop, and residual solvent-deasphalting oil material gets into in the deasphalting oil flash tank, realizes further separation between them with the help of pressure differential, and at this moment, 3-4 wt% solvent is separated out; preheating the residual solvent-deasphalted oil material to the operation temperature of a deasphalted oil stripping tower by a stripping tower preheater, stripping in the deasphalted oil stripping tower by using low-pressure steam, recovering the residual solvent, and feeding the solvent extracted from the deasphalted oil flash tank and the deasphalted oil stripping tower into a low-pressure solvent circulation pipeline.
3. The utility model discloses a solvent recovery system of supercritical solvent deasphalting process units can realize that the solvent more than 95 wt% separates out under supercritical state through deasphalting oil knockout tower in deasphalting oil-solvent mixture, and the later stage utilizes pressure differential to carry out the further separation that the solvent was realized in the flash distillation at deasphalting oil flash tank again, finally makes the solvent volume that needs superheated steam to strip at deasphalting oil stripping tower and carries out the steam greatly reduced to realize the purpose that reduces the energy consumption, the benefit of improvement system.
Drawings
FIG. 1 is a system flow diagram of a solvent recovery system of the apparatus of the present invention.
Reference numerals:
1-a first deasphalted oil-solvent feeding preheater, 2-a second deasphalted oil-solvent feeding preheater, a 3-deasphalted oil separation tower, a 4-deasphalted oil flash tank, a 5-stripping tower preheater, a 6-deasphalted oil stripping tower, a 7-deasphalted oil product pump, an 8-first flow valve, a 9-second flow valve and a 10-third flow valve.
Detailed Description
The present invention will be described in further detail with reference to specific examples, which are provided for illustrative purposes only, and are not intended to be limiting, and the scope of the present invention should not be limited thereby.
A solvent recovery system of a supercritical solvent deasphalting process device comprises a first deasphalted oil-solvent feeding preheater 1, a second deasphalted oil-solvent feeding preheater 2, a deasphalted oil separating tower 3, a deasphalted oil flash tank 4, a stripper preheater 5, a deasphalted oil stripper 6 and a deasphalted oil product pump 7, wherein a deasphalted oil-solvent feeding pipeline enters the deasphalted oil separating tower after passing through the first deasphalted oil-solvent feeding preheater and the second deasphalted oil-solvent feeding preheater, a solvent outlet pipeline at the top of the deasphalted oil separating tower is connected with a circulating solvent loop, a residual solvent-deasphalted oil mixed solution outlet pipeline at the bottom of the deasphalted oil separating tower is connected with the deasphalted oil flash tank, a solvent outlet at the top of the deasphalted oil flash tank is connected with a low-pressure solvent circulating pipeline and enters a low-pressure solvent circulating system, the bottom residual solvent-deasphalted oil mixed solution outlet pipeline of the deasphalted oil flash tank is connected to a deasphalted oil stripping tower through a stripping tower preheater, a solvent outlet pipeline at the top of the deasphalted oil stripping tower is connected with a low-pressure solvent circulating pipeline to enter a low-pressure solvent circulating system, a deasphalted oil product outlet pipeline is manufactured at the bottom of the deasphalted oil stripping tower, and a deasphalted oil product outlet pipeline is connected with a deasphalted oil product pump.
And a solvent outlet pipeline at the top of the deasphalted oil separation tower is connected with the first deasphalted oil-solvent feeding preheater and exchanges heat with the deasphalted oil-solvent feeding pipeline. The second deasphalted oil-solvent feeding preheater is connected with a heat transfer oil heat exchange pipeline.
And a first flow valve 8 is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil separation tower, and the first flow valve is in control connection with a first tower bottom liquid level sensor in the deasphalted oil separation tower.
And a second flow valve 9 is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil flash tank, and the second flow valve is in control connection with a second tower bottom liquid level sensor in the deasphalted oil flash tank.
And a third flow valve 10 is arranged on an outlet pipeline of the deasphalted oil product, and the third flow valve is controlled in a cascade mode by a third tower bottom liquid level sensor of the deasphalted oil stripping tower and a flow sensor behind a pump.
The working process of the solvent recovery system of the supercritical solvent deasphalting process device is as follows:
the solvent-deasphalted oil solution flows out from the top of an asphalt separating tower (not shown in the figure), exchanges heat with the top material of the deasphalted oil separating tower in a deasphalted oil-solvent feeding preheater, and recovers certain waste heat. Then, heat conducting oil is used in a deasphalted oil-solvent feeding preheater to further preheat the deasphalted oil-solvent feeding preheater, and finally, the supercritical solvent recovery condition is achieved.
Under the operating conditions of the deasphalted oil separation column, there are two streams, the supercritical solvent stream and the deasphalted oil-solvent stream. The supercritical condition can make the two fluids obtain the required density difference, thereby achieving good separation effect. The tower top pressure of the deasphalted oil separation tower is controlled by adjusting the solvent flow of the low-pressure solvent circulation pipeline. The operating temperature is controlled by the feed heater conduction oil flow.
The temperature of the solvent is raised above the critical temperature in order to provide the solvent with low density properties in this region. As the temperature is raised above the critical point, the density of the solvent decreases significantly to values close to the dense phase gas. Due to the increase in temperature, the deasphalted oil cannot be dissolved in the solvent and phase separation occurs. Due to the supercritical phase separation, about 95% of the solvent from the deasphalted oil-solvent mixture solution is recovered. The solvent separated here enters a high-pressure circulation loop to participate in the circulation of the solvent.
The mixed solution containing a small amount of solvent and deasphalted oil flows out from the bottom of the deasphalted oil separation tower and enters a deasphalted oil flash tank. The material flow is controlled by the liquid level at the bottom of the deasphalted oil separation tower. In the deasphalted oil flash tank, the pressure difference is fully utilized, so that about 2-4 wt% of solvent is flashed out and flows out from the top of the tank.
And the residual solvent-deasphalted oil solution flows out of the bottom of the deasphalted oil flash tank, and the flow rate of the residual solvent-deasphalted oil solution is controlled by the liquid level at the bottom of the deasphalted oil flash tank. The waste heat is preheated to the operation temperature of the stripping tower by a stripping tower preheater (heat is provided by heat conducting oil) and then enters the deasphalted oil stripping tower. Here, the contacting of the feed with superheated steam strips off the remaining solvent, allowing the deasphalted oil product to reach a low solvent content. Stripping steam enters the stripping tower from the bottom tray. The stripping steam rate is controlled by a flow. The temperature of the superheated steam should be equal to or higher than the operating temperature of the stripper. Cold steam may cool the deasphalted oil, affecting the stripping operation. The wet steam can create foam and affect the operation.
And the solvents extracted from the top of the deasphalted oil flash tank and the deasphalted oil stripping tower enter a low-pressure circulating solvent loop and enter a low-pressure circulating solvent system to participate in solvent circulation. The deasphalted oil product is extracted from the bottom of the deasphalted oil stripping tower, pumped by a deasphalted oil product pump and conveyed to the outside. The material flow is realized by cascade control of the liquid level at the bottom of the stripping tower and the flow after the pump.
The solvent recovery system of the supercritical solvent deasphalting process device enables more than 95 wt% of solvent to be separated out through the deasphalting oil separation tower in a supercritical state. And the further separation of the solvent is realized by flashing by utilizing pressure difference at the later stage, and finally, the amount of the solvent needing superheated steam stripping is greatly reduced. The energy consumption and the saving benefit are obvious, and the supercritical solvent deasphalting device has more benefits.
Although the embodiments of the present invention and the accompanying drawings have been disclosed for illustrative purposes, those skilled in the art will appreciate that various substitutions, alterations, and modifications are possible without departing from the spirit and scope of the invention and the appended claims, and thus the scope of the invention is not limited to the embodiments and drawings disclosed.
Claims (6)
1. A solvent recovery system of a supercritical solvent deasphalting process unit is characterized in that: the system comprises a first deasphalted oil-solvent feeding preheater, a second deasphalted oil-solvent feeding preheater, a deasphalted oil separation tower, a deasphalted oil flash tank, a stripper preheater, a deasphalted oil stripper and a deasphalted oil product pump, wherein a deasphalted oil-solvent feeding pipeline enters the deasphalted oil separation tower through the first deasphalted oil-solvent feeding preheater and the second deasphalted oil-solvent feeding preheater, a solvent outlet pipeline at the top of the deasphalted oil separation tower is connected with a circulating solvent loop, a residual solvent-deasphalted oil mixed solution outlet pipeline at the bottom of the deasphalted oil separation tower is connected with the deasphalted oil flash tank, a solvent outlet at the top of the deasphalted oil flash tank is connected with a low-pressure solvent circulating pipeline, a residual solvent-deasphalted oil mixed solution outlet pipeline at the bottom of the deasphalted oil flash tank is connected with the deasphalted oil flash tank through the preheater, the solvent outlet pipeline at the top of the deasphalted oil stripping tower is connected with a low-pressure solvent circulating pipeline, the deasphalted oil product outlet pipeline is arranged at the bottom of the deasphalted oil stripping tower, and the deasphalted oil product outlet pipeline is connected with a deasphalted oil product pump.
2. The solvent recovery system of a supercritical solvent deasphalting process unit according to claim 1, characterized in that: and a solvent outlet pipeline at the top of the deasphalted oil separation tower is connected with a first deasphalted oil-solvent feeding preheater and exchanges heat with the deasphalted oil-solvent feeding pipeline.
3. The solvent recovery system of a supercritical solvent deasphalting process unit according to claim 1, characterized in that: and the second deasphalted oil-solvent feeding preheater is connected with a heat conduction oil heat exchange pipeline.
4. The solvent recovery system of a supercritical solvent deasphalting process unit according to claim 1, characterized in that: and a first flow valve is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil separation tower, and the first flow valve is in control connection with a first tower bottom liquid level sensor in the deasphalted oil separation tower.
5. The solvent recovery system of a supercritical solvent deasphalting process unit according to claim 1, characterized in that: and a second flow valve is arranged on an outlet pipeline of the residual solvent-deasphalted oil mixed solution at the bottom of the deasphalted oil flash tank, and the second flow valve is in control connection with a second tower bottom liquid level sensor in the deasphalted oil flash tank.
6. The solvent recovery system of a supercritical solvent deasphalting process unit according to claim 1, characterized in that: and a third flow valve is arranged on the deasphalted oil product outlet pipeline, and the third flow valve is controlled in a cascade mode by a third tower bottom liquid level sensor of the deasphalted oil stripping tower and a flow sensor behind the pump.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115717082A (en) * | 2021-08-24 | 2023-02-28 | 中国石油化工股份有限公司 | Method and system for recovering solvent deasphalting waste heat |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115717082A (en) * | 2021-08-24 | 2023-02-28 | 中国石油化工股份有限公司 | Method and system for recovering solvent deasphalting waste heat |
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