Efficient evaporation desolventizing system of oil leaching device

Abstract

The utility model provides an efficient evaporation desolventizing system of an oil leaching device, which comprises a first evaporator, a primary steaming crude oil delivery pump, a pre-secondary evaporator, a pre-secondary steaming crude oil delivery pump, a second evaporator, a secondary steaming crude oil delivery pump, a vacuum desolventizing tank and a crude oil delivery pump which are sequentially connected through pipelines, an outlet of the crude oil delivery pump is connected with a shell side inlet of the pre-secondary evaporator, and a shell side outlet of the pre-secondary evaporator is connected to the crude oil cooling equipment; the first evaporator, the pre-secondary evaporator and the second evaporator are respectively connected with a vacuum system; the vacuum desolventizing tank is provided with a first high vacuum system and a second high vacuum system which are connected in parallel through a pipeline. According to the mixed oil heat energy recovery circulation loop system, the use amount of heating steam of the system is reduced, meanwhile, the cooling cost of discharged crude oil is reduced, meanwhile, the evaporation efficiency of the mixed oil is improved, the use amount of direct steam is reduced, and generation of harmful substances is avoided.

Description

Technical Field

[0001] The utility model relates to the field of oil processing, in particular to an efficient evaporation and solvent stripping system for an oil leaching device. Background Art

[0002] The basic process of oil production by an oil leaching device is to use an organic solvent to extract and leach the pretreated oil materials to obtain mixed oil containing a large amount of solvent and wet meal. Among them, the mixed oil is evaporated and distilled to obtain crude oil, and the wet meal is evaporated and dried to produce the finished meal required for feed. The solvent gas obtained by evaporation and drying is recycled after condensation and cooling. The above leaching process is mainly divided into four parts: oil leaching, mixed oil evaporation, wet meal stripping, and solvent recovery.

[0003] Mixed oil evaporation is a process of using indirect steam to heat the mixed oil to its boiling point, vaporizing the solvent, and concentrating the mixed oil. The boiling point of the mixed oil decreases with the decrease of the operating pressure and increases with the increase of the mixed oil concentration. Therefore, carrying out mixed oil evaporation under negative pressure can ensure the quality of the oil. When the concentration of the mixed oil reaches a certain level, the boiling point rises sharply. At this time, direct steam is needed to strip the mixed oil to further remove the solvent. After evaporation and stripping of the mixed oil, the residual solvent content is required to be below 50 ppm.

[0004] Mixed oil evaporation and stripping are an important link in oil leaching production. It not only determines the quality of the crude oil but also plays an important role in steam consumption. Therefore, on the premise of effectively removing the solvent in the mixed oil, minimizing the steam consumption has been increasingly emphasized in the mixed oil treatment process.

[0005] In the prior art, the "mixed oil evaporation and solvent stripping system" with the authorized announcement number of CN214088436U mainly uses a stripping tower, which consumes a large amount of direct steam and is too energy-consuming. Summary of the Utility Model

[0006] The purpose of the utility model is to provide an efficient evaporation and solvent stripping system for an oil leaching device. During the evaporation and solvent stripping process of the mixed oil, a high vacuum system is adopted and heat energy is recycled. By replacing or reducing some equipment with higher costs, the steam consumption is reduced.

[0007] To achieve the above object, the present utility model provides an efficient evaporation and desolventization system for an oil leaching device, which includes a first evaporator connected to the mixed oil pipeline of the oil leaching section, and includes a first evaporator, a primary second evaporation crude oil transfer pump, a pre-secondary evaporation, a pre-secondary evaporation crude oil transfer pump, a second evaporator, a secondary evaporation crude oil transfer pump, a vacuum desolventization tank, and a crude oil transfer pump connected in sequence through pipelines. The outlet of the crude oil transfer pump is connected to the inlet of the shell side of the pre-secondary evaporation, and the outlet of the shell side of the pre-secondary evaporation is connected to an oil cooling device; the first evaporator, the pre-secondary evaporation, and the second evaporator are respectively connected to a vacuum system; the vacuum desolventization tank is provided with a parallel first high-vacuum system and a second high-vacuum system through pipelines.

[0008] Further, in the efficient evaporation and desolventization system of the oil leaching device, the first high-vacuum system includes a steam jet pump and a steam superheater. The top gas phase outlet of the vacuum desolventization tank is connected to the steam jet pump, the exhaust port of the steam jet pump is connected to the inlet of the tube side of the steam superheater, and the outlet of the tube side of the steam superheater is connected to the buffer tank of the second evaporator.

[0009] Further, in the efficient evaporation and desolventization system of the oil leaching device, the inlet of the shell side of the steam superheater is connected to a heating steam pipeline, and the outlet of the shell side is connected to a condensate pipeline.

[0010] Further, in the efficient evaporation and desolventization system of the oil leaching device, the second high-vacuum system includes a plate heat exchanger and a liquid ring vacuum pump. The top gas phase outlet of the vacuum desolventization tank is connected to the inlet of the hot side of the plate heat exchanger, the outlet of the hot side of the plate heat exchanger is connected to the inlet of the liquid ring vacuum pump, and the exhaust port of the liquid ring vacuum pump is connected to a tail gas treatment system.

[0011] Further, in the efficient evaporation and desolventization system of the oil leaching device, the cold side of the plate heat exchanger is connected to a cooling water / frozen water pipeline, and solvent recovery pipelines are respectively provided at the outlet of the hot side of the plate heat exchanger and the outlet of the liquid ring vacuum pump.

[0012] Further, in the efficient evaporation and desolventization system of the oil leaching device, a flash tank is provided at the upper end of the first evaporator, and a flash tank is provided at the lower end of the pre-secondary evaporation; a vacuum tank is provided at the upper end of the second evaporator, and a buffer tank is provided at the lower end.

[0013] Further, in the efficient evaporation and desolventization system of the oil leaching device, the buffer tank of the second evaporator and the bottom end of the vacuum desolventization tank are respectively connected to a direct steam pipeline.

[0014] Furthermore, in the high-efficiency evaporation and solvent stripping system of the oil leaching device, the first evaporator is a rising film evaporator, the pre-secondary evaporator is a falling film evaporator, and the second evaporator is a falling film evaporator.

[0015] Furthermore, in the high-efficiency evaporation and solvent stripping system of the oil leaching device, the shell-side inlet of the first evaporator is connected to the DT secondary steam pipeline, and the shell-side outlet is connected to the condensate pipeline; the shell-side inlet of the second evaporator is connected to the heating steam pipeline, and the shell-side outlet is connected to the condensate pipeline.

[0016] Compared with the prior art, the beneficial effects of the present utility model are mainly reflected in: through the designed mixed oil heat energy recovery circulation loop system, the heat energy of the discharged crude oil from the vacuum solvent stripping tank is recovered, so that the solvent in the first-evaporated crude oil is further evaporated, and the discharged crude oil from the vacuum solvent stripping tank is cooled. While reducing the usage amount of the system heating steam, the cooling cost of the discharged crude oil is reduced.

[0017] Compared with the prior art, the present utility model has the following advantages:

[0018] (1) For different solvent contents in the mixed oil, multiple vacuum systems and high-vacuum systems are designed in sections to effectively reduce the solvent content of the mixed oil with different solvent contents in sections. Since the solvent contents of the mixed oil in the first evaporator, the pre-secondary evaporator, the second evaporator and the vacuum solvent stripping tank gradually decrease, the vacuum degree of the second evaporator is better than that of the first evaporator and the pre-secondary evaporator, and the vacuum degree of the vacuum solvent stripping tank is better. A better vacuum degree can reduce the boiling point of the mixed oil, which not only improves the evaporation efficiency of the mixed oil, saves the usage amount of direct steam, but also effectively avoids a series of harmful substances generated by the oil due to high temperature.

[0019] (2) The stripping tower that requires a large amount of direct steam is abandoned, and instead, a combined design of the pre-secondary evaporator and the vacuum solvent stripping tank is adopted. The new design can save about 70% of the direct steam and reduce the solvent content in the mixed oil from the oil leaching section to less than 50 ppm.

[0020] (3) A mixed oil heat energy recovery circulation loop system is designed to recover the heat energy of the discharged crude oil from the vacuum solvent stripping tank, so that the solvent in the first-evaporated crude oil is further evaporated, and the discharged crude oil from the vacuum solvent stripping tank is cooled. While reducing the usage amount of the system heating steam, the cooling cost of the discharged crude oil is reduced.

[0021] (4) The vacuum desolventizing tank of the utility model is equipped with two sets of parallel high vacuum systems. The first high vacuum system extracts the gas from the vacuum desolventizing tank through a steam jet pump, and after being superheated by a steam superheater, generates low-pressure superheated steam, which serves as the stripping steam for the second evaporator, thereby realizing the recovery and reuse of heat energy. Among them, the use of the steam superheater can not only effectively remove the moisture in the mixed gas and avoid the gelling of the mixed oil, but also increase the temperature of the mixed gas to achieve a better stripping effect. The second high vacuum system uses a plate heat exchanger instead of a traditional shell and tube heat exchanger, and is combined with a liquid ring vacuum pump to achieve high vacuum. The plate heat exchanger has a better heat exchange effect than the shell and tube heat exchanger, and has a low maintenance cost and a low cost.

[0022] (5) The design of the second evaporator of the utility model has been upgraded. In addition to the above-mentioned second evaporator lower end buffer tank with direct steam for stripping the solvent in the mixed oil, a vacuum tank with a larger diameter is installed on the top of the second evaporator. This design is to reduce the gas velocity and prevent the solvent gas from carrying oil when the stripping gas enters the vacuum system. The solvent is recovered and then enters the extractor to spray and soak the embryo slices. The presence of oil will lead to an increase in the oil content in the meal, affecting the yield of the extracted crude oil.

[0023] (6) The utility model system fully optimizes the design and replaces or reduces some of the equipment with higher costs. Both the initial investment cost and the later operation and maintenance cost are lower. In terms of energy saving and consumption reduction, the utility model system actively responds to the national call to save energy and creates considerable and sustainable economic benefits for the users. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] Figure 1 The utility model is a schematic diagram of the structure of the high-efficiency evaporation and desolventizing system of the oil extraction device. DETAILED DESCRIPTION

[0025] The following will be described in more detail with reference to the schematic diagram of the efficient evaporation desolventizing system of the oil extraction device of the utility model, wherein the preferred embodiment of the utility model is shown, and it should be understood that the utility model described herein can be modified by those skilled in the art, while still achieving the advantageous effects of the utility model. Therefore, the following description should be understood as being widely known to those skilled in the art, and not as a limitation to the utility model.

[0026] In the description of the present utility model, it should be noted that for the orientation terms, such as the terms "center", "horizontal", "longitudinal", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", etc., the indicated orientation and position relationship are based on the orientation or position relationship shown in the drawings. It is only for the convenience of describing the present utility model and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and should not be construed as limiting the specific protection scope of the present utility model.

[0027] In addition, the terms "first" and "second" are only used for descriptive purposes and should not be construed as indicating or implying relative importance or implicitly specifying the quantity of technical features. Thus, the features defined with "first" and "second" may explicitly or implicitly include one or more of such features. In the description of the present utility model, the meaning of "at least" is one or more than one, unless otherwise specifically defined.

[0028] In the following paragraphs, the present utility model will be described more specifically by way of example with reference to the drawings. According to the following description, the advantages and features of the present utility model will be clearer. It should be noted that the drawings are all in a very simplified form and use non-precise scales, and are only used to conveniently and clearly assist in explaining the purpose of the embodiments of the present utility model.

[0029] As Figure 1 shown, the present utility model provides an efficient evaporation and desolventization system for an oil leaching device. The first evaporator is connected to the mixed oil pipeline from the oil leaching section, and includes a first evaporator 1, a first evaporation crude oil transfer pump 2, a pre-second evaporator 3, a pre-second evaporation crude oil transfer pump 4, a second evaporator 5, a second evaporation crude oil transfer pump 6, a vacuum desolventization tank 7, and a crude oil transfer pump 8 connected in sequence through pipelines. The outlet of the crude oil transfer pump 8 is connected to the inlet of the shell side of the pre-second evaporator 3, and the outlet of the shell side of the pre-second evaporator 3 is connected to the crude oil cooling device; the first evaporator 1, the pre-second evaporator 3, and the second evaporator 5 are respectively connected to a vacuum system; the vacuum desolventization tank 7 is provided with a first high-vacuum system and a second high-vacuum system connected in parallel.

[0030] Specifically, the tube side outlet of the first evaporator 1, that is, the flash tank of the first evaporator 1 is connected to the inlet of the first evaporation crude oil transfer pump 2. The outlet of the first evaporation crude oil transfer pump 2 is connected to the tube side inlet of the pre-second evaporation device 3. The tube side outlet of the pre-second evaporation device 3, that is, the flash tank of the pre-second evaporation device 3 is connected to the inlet of the pre-second evaporation crude oil transfer pump 4. The outlet of the pre-second evaporation crude oil transfer pump 4 is connected to the tube side inlet of the second evaporator 5. The tube side outlet of the second evaporator 5 is connected to the inlet of the second evaporation crude oil transfer pump 6. The outlet of the second evaporation crude oil transfer pump 6 is connected to the feed inlet of the vacuum stripping tank 7. The discharge outlet at the bottom of the vacuum stripping tank 7 is connected to the inlet of the crude oil transfer pump 8. The outlet of the crude oil transfer pump 8 is connected to the shell side inlet of the pre-second evaporation device 3. The shell side outlet of the pre-second evaporation device 3 is connected to the crude oil cooling equipment, forming a heat energy recovery circulation loop for the miscella. Through the heat energy recovery circulation loop system for the miscella, the heat energy of the discharged crude oil from the vacuum stripping tank 7 is recovered, and in cooperation with the pre-second evaporation device 3, the solvent in the first evaporation crude oil of the first evaporator 1 is further evaporated, and the discharged crude oil from the vacuum stripping tank 7 is correspondingly cooled. It realizes reducing the usage amount of the system heating steam while reducing the cooling cost of the discharged crude oil.

[0031] Furthermore, as Figure 1 shown, a flash tank is provided at the upper end of the first evaporator 1, and a flash tank is provided at the lower end of the pre-second evaporation device 3; a vacuum tank is provided at the upper end of the second evaporator 5, and a buffer tank is provided at the lower end. Preferably, the first evaporator 1 is a rising film evaporator, the pre-second evaporation device 3 is a falling film evaporator, and the second evaporator 5 is a falling film evaporator.

[0032] Meanwhile, the first evaporator 1, the pre-second evaporation device 3, and the second evaporator 5 are respectively connected to a vacuum system, that is, the flash tanks of the first evaporator 1 and the pre-second evaporation device 3 are both connected to the vacuum system, and the vacuum tank of the second evaporator 5 is connected to the vacuum system; the top of the vacuum stripping tank 7 is configured with two mutually backup first high-vacuum systems and second high-vacuum systems in parallel through pipelines. In this application, through the segmented design of multiple vacuum systems and high-vacuum systems, the solvent content of the miscella with different solvent contents is effectively reduced in segments. Therefore, the vacuum degree of the second evaporator 5 is better than that of the first evaporator 1 and the pre-second evaporation device 3, and the vacuum degree of the vacuum stripping tank 7 is even better. By reducing the boiling point of the miscella through a better vacuum degree, not only the evaporation efficiency of the miscella is improved, the usage amount of direct steam is saved, but also a series of harmful substances generated by the grease due to high temperature are effectively avoided.

[0033] Furthermore, as Figure 1As shown in the figure, the first high-vacuum system includes a steam jet pump 9 and a steam superheater 10. The top gas-phase outlet of the vacuum desolventizing tank 7 is connected to the steam jet pump 9 through a pipeline. The exhaust port of the steam jet pump 9 is connected to the tube-side inlet of the steam superheater 10. The tube-side outlet of the steam superheater 10 is connected to the buffer tank at the lower end of the second evaporator 5. At the same time, the shell-side inlet of the steam superheater 10 is connected to the heating steam pipeline, and the shell-side outlet is connected to the condensate pipeline. Therefore, the first high-vacuum system extracts the gas in the vacuum desolventizing tank 7 through the steam jet pump 9, and after being superheated by the steam superheater 10, low-pressure superheated steam is generated, which is used as the stripping steam of the second evaporator 5, thus realizing the recycling and reuse of thermal energy. Among them, the use of the steam superheater 10 can not only effectively remove the moisture in the mixed gas, avoid the gumming of the mixed oil, but also increase the temperature of the mixed gas to achieve a better stripping effect.

[0034] Furthermore, as Figure 1 shown, the second high-vacuum system includes a plate heat exchanger 11 and a liquid ring vacuum pump 12. The top gas-phase outlet of the vacuum desolventizing tank 7 is connected to the hot-side inlet of the plate heat exchanger 11 through a pipeline. The hot-side outlet of the plate heat exchanger 11 is connected to the inlet of the liquid ring vacuum pump 12. The exhaust port of the liquid ring vacuum pump 12 is connected to the tail gas treatment system. Among them, the cold side of the plate heat exchanger 11 is connected with a cooling water / frozen water pipeline, and solvent recovery pipelines are respectively provided at the hot-side outlet of the plate heat exchanger 11 and the outlet of the liquid ring vacuum pump 12. Since the second high-vacuum system uses a plate heat exchanger 11 instead of a traditional shell-and-tube heat exchanger, its combination with the liquid ring vacuum pump 12 can achieve a high-vacuum effect, that is, the plate heat exchanger 11 has a better heat exchange effect, lower maintenance cost and cheaper cost than the shell-and-tube heat exchanger.

[0035] In addition, as Figure 1 shown, the bottom end of the buffer tank of the second evaporator 5 is connected to the direct steam pipeline. Since the design of the second evaporator 5 has been upgraded, in addition to the direct steam passing through the buffer tank at the lower end of the second evaporator 5 for stripping the solvent in the mixed oil, a vacuum tank with a larger diameter is also installed at the top of the second evaporator 5. The gas velocity is effectively reduced to avoid the entrainment of oil fines by the solvent gas when the stripping gas enters the vacuum system. After the solvent is recovered, it enters the leaching tank to spray and soak the embryo slices. The presence of oil fines will cause an increase in the oil content in the meal and affect the yield of the leached crude oil. At the same time, the bottom end of the vacuum desolventizing tank 7 is connected to the direct steam pipeline.

[0036] Furthermore, as Figure 1 shown, the shell-side inlet of the first evaporator 1 is connected to the DT secondary steam pipeline, and the shell-side outlet is connected to the condensate pipeline; the shell-side inlet of the second evaporator 5 is connected to the heating steam pipeline, and the shell-side outlet is connected to the condensate pipeline.

[0037] The utility model system fully optimizes the design and replaces or reduces some of the equipment with higher cost. Both the initial investment cost and the later operation and maintenance cost are lower. In terms of energy saving and consumption reduction, the utility model system actively responds to the national call to save energy and creates considerable and sustainable economic benefits for the user.

[0038] Here’s how it works:

[0039] After pretreatment, the oil enters the oil extraction section, where it is soaked by solvent spraying and leaching to obtain a mixed oil with a concentration of 30% to 40%. The mixed oil enters the first evaporator 1 from the bottom, and the mixed oil goes through the tube side, and the DT secondary steam goes through the shell side. Under vacuum conditions, most of the solvent in the mixed oil evaporates, and the concentration of the mixed oil increases to 70% to 90%. It is pumped to the tube side of the top of the pre-secondary distillation 3 by the first distillation crude oil delivery pump 2, and heat is exchanged with the discharged crude oil of the vacuum desolventizing tank 7, and the temperature increases. Under the same vacuum conditions, the solvent is further evaporated to obtain 85% to 95% of the pre-secondary distillation crude oil. It is then pumped to the tube side of the second evaporator 5 by the pre-secondary distillation crude oil delivery pump 4, and heating steam is introduced into the shell side. Under the action of gravity, the mixed oil flows downward in a film-like manner along the tube array to the buffer tank at the lower end of the second evaporator 5, and is directly steam stripped. Under better vacuum conditions, the solvent evaporates and vaporizes again. Since the solvent content in the second distilled crude oil is very low, it is pumped to the vacuum desolventizing tank 7 through the second distilled crude oil delivery pump 6, and the two sets of high vacuum systems connected thereto can achieve a good vacuum degree. At this time, only a small amount of direct steam needs to be introduced into the vacuum desolventizing tank 7 to obtain crude oil with a temperature of 85°C to 105°C and a residual solvent of less than 50ppm. After the crude oil is discharged from the bottom of the vacuum desolventizing tank 7, it is pumped to the shell side inlet of the pre-second distillation 3 through the crude oil delivery pump 8, and heat is exchanged with the first distilled crude oil, and the temperature is reduced to 65°C to 85°C, and finally cooled and stored.

[0040] The top of the vacuum desolventizing tank 7 is connected to two parallel vacuum systems. In the first high vacuum system, the steam jet pump 9 uses medium-pressure steam as the motive steam, which is ejected at high speed after entering the nozzle to generate low pressure, and the gas in the vacuum desolventizing tank 7 is sucked into the mixing chamber and mixed, and then discharged from the exhaust port. The mixed gas containing a small amount of solvent and water droplets is heated by the steam superheater 10 to generate low-pressure superheated steam, which can be used as direct stripping steam for the second evaporator 5. Considering that the solvent in the mixed gas will affect the stripping effect, a small amount of fresh direct steam will be added. In the second high vacuum system, the gas in the vacuum desolventizing tank 7 passes through the plate heat exchanger 11, exchanges heat with cooling water / chilled water, and the temperature is reduced, and then it is pumped out to the tail gas treatment system through the liquid ring vacuum pump 12. Among them, the solvent in the gas is condensed into liquid to remove the solvent and recover it.

[0041] In summary, in this embodiment, the efficient evaporation and solvent stripping system of the oil leaching device proposed herein recovers the heat energy of the crude oil discharged from the vacuum solvent stripping tank through the designed heat energy recovery and circulation loop system for the miscella, further evaporating the solvent in the first-stage evaporated crude oil and cooling the crude oil discharged from the vacuum solvent stripping tank. This achieves a reduction in the consumption of heating steam in the system while reducing the cooling cost of the discharged crude oil. At the same time, through the multiple vacuum systems and high-vacuum systems designed in sections, the solvent content of the miscella with different solvent contents is effectively reduced in sections. By reducing the boiling point of the miscella through the vacuum degree, not only is the evaporation efficiency of the miscella improved, the consumption of direct steam is saved, but also a series of harmful substances generated by the oil due to high temperature are effectively avoided.

[0042] Compared with the prior art, the present utility model abandons the stripping column that requires a large amount of direct steam consumption and replaces it with a combined design of a pre-second evaporation and a vacuum solvent stripping tank. The new design can save about 70% of the direct steam and reduce the solvent content in the miscella to below 50 ppm.

[0043] The above are only the preferred embodiments of the present utility model and do not impose any limitation on the present utility model. Any person skilled in the art within the technical field, without departing from the scope of the technical solution of the present utility model, makes any form of equivalent substitution or modification and other changes to the technical solution and technical content disclosed by the present utility model, all of which fall within the content of the technical solution of the present utility model and still belong to the protection scope of the present utility model.

Claims

1. An efficient evaporation and desolventizing system for an oil extraction device, comprising a first evaporator connected to a mixed oil pipeline of an oil extraction section, characterized in that: The invention comprises a first evaporator (1), a crude oil delivery pump (2), a pre-secondary evaporator (3), a crude oil delivery pump (4), a second evaporator (5), a crude oil delivery pump (6), a vacuum desolventizing tank (7) and a crude oil delivery pump (8) which are sequentially connected via pipelines, wherein the outlet of the crude oil delivery pump (8) is connected to the shell side inlet of the pre-secondary evaporator (3), and the shell side outlet of the pre-secondary evaporator (3) is connected to a crude oil cooling device; the first evaporator (1), the pre-secondary evaporator (3) and the second evaporator (5) are respectively connected to vacuum systems; and the vacuum desolventizing tank (7) is provided with a first high vacuum system and a second high vacuum system connected in parallel via pipelines.

2. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 1 is characterized in that: The first high vacuum system comprises a steam jet pump (9) and a steam superheater (10); the top gas phase outlet of the vacuum desolventizing tank (7) is connected to the steam jet pump (9); the exhaust port of the steam jet pump (9) is connected to the pipe side inlet of the steam superheater (10); and the pipe side outlet of the steam superheater (10) is connected to the buffer tank of the second evaporator (5).

3. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 2 is characterized in that: The shell side inlet of the steam superheater (10) is connected to a heating steam pipeline, and the shell side outlet is connected to a condensate water pipeline.

4. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 1 is characterized in that: The second high vacuum system comprises a plate heat exchanger (11) and a liquid ring vacuum pump (12); the top gas phase outlet of the vacuum desolventizing tank (7) is connected to the hot side inlet of the plate heat exchanger (11); the hot side outlet of the plate heat exchanger (11) is connected to the inlet of the liquid ring vacuum pump (12); and the exhaust port of the liquid ring vacuum pump (12) is connected to the exhaust gas treatment system.

5. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 4 is characterized in that: The cold side of the plate heat exchanger (11) is connected to a cooling water / chilled water pipeline, and the hot side outlet of the plate heat exchanger (11) and the outlet of the liquid ring vacuum pump (12) are respectively provided with solvent recovery pipelines.

6. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 1 is characterized in that: The upper end of the first evaporator (1) is provided with a flash box, and the lower end of the pre-secondary evaporator (3) is provided with a flash box; the upper end of the second evaporator (5) is provided with a vacuum tank, and the lower end is provided with a buffer tank.

7. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 6, characterized in that: The bottom ends of the buffer tank of the second evaporator (5) and the vacuum desolventizing tank (7) are respectively connected to direct steam pipelines.

8. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 1 is characterized in that: The first evaporator (1) is a rising film evaporator, the pre-secondary evaporator (3) is a falling film evaporator, and the second evaporator (5) is a falling film evaporator.

9. The high-efficiency evaporation and desolventizing system of the oil extraction device according to claim 1, characterized in that: The shell side inlet of the first evaporator (1) is connected to the DT secondary steam pipeline, and the shell side outlet is connected to the condensate water pipeline; the shell side inlet of the second evaporator (5) is connected to the heating steam pipeline, and the shell side outlet is connected to the condensate water pipeline.

Images