CN214088436U - Mixed oil evaporation desolventizing system - Google Patents
Mixed oil evaporation desolventizing system Download PDFInfo
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- CN214088436U CN214088436U CN202022813647.XU CN202022813647U CN214088436U CN 214088436 U CN214088436 U CN 214088436U CN 202022813647 U CN202022813647 U CN 202022813647U CN 214088436 U CN214088436 U CN 214088436U
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Abstract
The utility model relates to a miscella evaporation desolventizing system, include the first evaporimeter that links to each other with the miscella input tube, the discharge gate of first evaporimeter links to each other with the entry of one evaporation pump, the export of one evaporation pump links to each other with the shell side entry of miscella heat exchanger, the shell side export of miscella heat exchanger links to each other with the feed inlet that two evaporate in advance before with, the discharge gate that two evaporate in advance before with the feed inlet that two evaporate in advance after links to each other, the discharge gate that two evaporate in advance after links to each other with the feed inlet of second evaporimeter, the discharge gate of second evaporimeter links to each other with the entry of two evaporation pumps, the export of two evaporation pumps links to each other with the feed inlet of strip tower, the bottom export of strip tower links to each other with the entry of strip pump, the export of strip pump links to each other with the tube side entry of miscella heat exchanger, the tube side export of miscella heat exchanger links to each other with the miscella output tube. The exhausted steam of the first evaporator and the second evaporator is sent to a shell pass of the second evaporator through an evaporation condenser and an evaporation jet pump. The system has high heat recovery efficiency and low steam consumption.
Description
Technical Field
The utility model relates to an evaporating system, in particular to miscella evaporation desolventizing system belongs to grease extraction technical field.
Background
The oil extraction workshop comprises a leaching working section, a wet meal desolventizing working section, a mixed oil evaporating working section and a mineral oil absorbing working section. In the mixed oil evaporation section, the mixed oil passes through the first evaporator, the second evaporator and the stripping tower to obtain qualified crude oil. The first evaporator concentrates the mixed oil to 75-85%; the second evaporator concentrates the mixed oil to 95% -97%; the stripping tower uses steam as direct steam to strip the mixed oil from the second evaporator, and the content of the oil is reduced to below 50 ppm.
Both the mixed oil evaporation and stripping were performed under vacuum. Wherein the first evaporator and the second evaporator share one vacuum system, and the vacuum degree is controlled to be 40-60 KPa; the stripping tower is provided with a single vacuum system, and the vacuum degree is controlled to be 50-70 KPa. The gas phase temperature of the first evaporator is 50-58 ℃, the gas phase outlet temperature of the second evaporator is 100-110 ℃, and the gas phase outlet temperature of the stripping tower is 100-110 ℃. The evaporation vacuum system consists of an evaporation condenser and an evaporation jet pump; the vacuum system of the stripping tower consists of a stripping condenser and a stripping jet pump. The steam jet pump adopts 6-10bar steam as power steam to pump out uncondensed air and hexane in the front condenser, and the outlet of the steam jet pump is mixed gas of the steam, the air and the hexane. The mixed gas has high water vapor and hexane content, high temperature over 100 deg.c and high heat recovering value.
At present, mixed gas at the outlet of the jet pump is mixed with gas phase of the evapo-separated machine to be used as a heat source for primary evaporation. The gas phase of the desolventizer-toaster is usually 72-78 ℃ and is lower than the temperature of the mixed gas at the outlet of the jet pump, and the gas phase and the mixed gas are mixed to reduce the temperature of the mixed gas at the outlet of the jet pump, thereby reducing the quality of the mixed gas at the outlet of the jet pump. In addition, the heat of the gas phase of the evaporator is large enough to meet the heat requirement of the first evaporator, and the mixed gas at the outlet of the jet pump is merged into the gas phase of the evaporator, so that the heat of the mixed gas at the outlet of the jet pump is not fully utilized, the steam quantity required by subsequent evaporation is increased, and the load of a subsequent condenser is increased.
The temperature of the gas phase outlets of the second evaporator and the stripping tower is over 100 ℃, so that the utilization value is high, a large amount of heat is wasted by directly condensing in the vacuum condenser, and the load of the condenser is increased.
In summary, the existing mixed oil evaporation and desolventization process generally has the following defects: (1) high-quality jet gas and relatively low-quality steam-stripping machine are not separated, so that the temperature difference in the heat exchange process is reduced, the concentration of the mixed oil before entering the second evaporator is relatively low, and the steam consumption of the second evaporator is increased; (2) the vacuum ejector pump, the second evaporator and the steam stripping condenser are insufficient in gas phase heat utilization, a large amount of heat enters the condenser, and the load of the subsequent condenser is increased.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to overcome the problem that exists among the prior art, provide a miscella evaporation desolventizing system, heat recovery efficiency is high, and steam consumption is low.
In order to solve the technical problem, the mixed oil evaporation desolventizing system of the utility model comprises a first evaporator connected with a mixed oil input pipe, the discharge hole of the first evaporator is connected with the inlet of an evaporation and extraction pump, the outlet of the evaporation and extraction pump is connected with the shell pass inlet of the mixed oil heat exchanger, the shell pass outlet of the mixed oil heat exchanger is connected with the feed inlet of the front pre-secondary evaporation, the discharge outlet of the front pre-secondary evaporation is connected with the feed inlet of the rear pre-secondary evaporation, the discharge hole of the back pre-secondary evaporation is connected with the feed hole of a second evaporator, the discharge hole of the second evaporator is connected with the inlet of a secondary evaporation pump, the outlet of the secondary evaporation pump is connected with the feed inlet of the stripping tower, the outlet at the bottom of the stripping tower is connected with the inlet of the stripping pump, and the outlet of the stripping pump is connected with the tube pass inlet of the mixed oil heat exchanger, and the tube pass outlet of the mixed oil heat exchanger is connected with the mixed oil output pipe.
As the improvement of the utility model, the shell side steam inlet of first evaporimeter links to each other with the desolventizer-toaster gas phase pipe, and the top steam vent of first evaporimeter and the top steam vent that two after evaporate in advance all link to each other with evaporative condenser's entry, evaporative condenser's steam vent links to each other with evaporative jet pump's induction port, evaporative jet pump's mixed steam outlet with two after evaporate shell side steam inlet in advance link to each other.
As a further improvement of the utility model, the top steam vent of second evaporimeter with the top steam vent of strip tower all with the shell side steam inlet that two were evaporated in advance links to each other before, the shell side steam outlet that two were evaporated in advance links to each other with the shell side entry of strip precondenser before, the shell side condensate export that two were evaporated in advance links to each other with the knockout drum before, the tube side of strip precondenser links to each other with fresh solvent pipe, the shell side steam vent of strip precondenser links to each other with the entry of strip condenser, the shell side steam vent of strip condenser links to each other with the induction port of strip jet pump, the mixed steam outlet of strip jet pump also with the shell side steam inlet that two were evaporated in advance after links to each other.
Compared with the prior art, the utility model discloses following beneficial effect has been obtained: 1. feeding the mixed oil with the concentration of 25-30% wt into a first evaporator from a mixed oil input pipe for evaporation, heating the first evaporator to 55-60 ℃, and increasing the concentration to 75-85% wt; and then sending the first-steaming mixed oil into a mixed oil heat exchanger by a first steaming extraction pump, heating the mixed oil by the first pre-steaming after the oil temperature is increased to 70-75 ℃, heating the mixed oil to 80-85 ℃ by the second pre-steaming, heating the mixed oil to 90-95 ℃ by the second pre-steaming, then sending the mixed oil into a second evaporator to be heated to 105-110 ℃ for evaporation, increasing the concentration of the mixed oil to 95-97 wt%, and finally sending the mixed oil into a stripping tower to increase the concentration to more than 99.995 wt%.
2. The first evaporator uses the waste heat of the previous desolventizer-toaster as a heat source, the outlet of the mixed oil heat exchanger is provided with the previous pre-secondary steaming, the mixed oil at the outlet of the mixed oil heat exchanger is heated by using the heat of the gas phases of the second evaporator and the stripper, the temperature of the mixed oil can be increased by 5-10 ℃, the steam consumption of the second evaporator can be saved, and the steam consumption can be reduced by 1.5-3kg per ton of oil material.
3. Outlets of the evaporation jet pump and the stripping jet pump are connected with a shell pass inlet of the back pre-secondary evaporation, mixed oil at the back pre-secondary evaporation outlet is heated by using heat of mixed gas of the jet pump, the temperature of the mixed oil is continuously increased by 5-15 ℃, steam consumption of the second evaporator can be further saved, and the steam consumption can be reduced by 1.5-4.5kg per ton of oil.
4. The mixed gas at the gas phase outlet of the front two-stage pre-evaporation shell pass is used for heating the fresh solvent through the stripping pre-condenser, so that the steam consumption of the solvent heater can be saved, and the steam consumption can be reduced by 3-6kg per ton of oil.
Drawings
The invention will be described in further detail with reference to the drawings and the detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.
Fig. 1 is a flow chart of the mixed oil evaporation desolventizing system of the utility model.
In the figure: 1. a first evaporator; 2. a mixed oil heat exchanger; 3. pre-steaming for the second time; 4. then pre-steaming for the second time; 5. a second evaporator; 6. a stripping column; 7. an evaporative condenser; 8. a stripping precondenser; 9. a stripping condenser; 10. an evaporative jet pump; 11. a stripping jet pump; p1, a steam extraction pump; p2, a second evaporation pump; p3, a stripping pump; G1. a mixed oil input pipe; G2. a vapor phase pipe of the desolventizer-toaster; G3. a mixed oil output pipe; G4. a fresh solvent tube; G5. a raw steam pipe.
Detailed Description
As shown in figure 1, the mixed oil evaporation desolventizing system of the utility model comprises a first evaporator 1, a mixed oil heat exchanger 2, a front pre-secondary evaporation 3, a rear pre-secondary evaporation 4, a second evaporator 5 and a stripping tower 6, wherein the first evaporator 1 is connected with a mixed oil input pipe G1, a discharge port of the first evaporator 1 is connected with an inlet of a first evaporation pump P1, an outlet of the first evaporation pump P1 is connected with a shell pass inlet of the mixed oil heat exchanger 2, a shell pass outlet of the mixed oil heat exchanger 2 is connected with a feed port of the front pre-secondary evaporation 3, a discharge port of the front pre-secondary evaporation 3 is connected with a feed port of the rear pre-secondary evaporation 4, a discharge port of the rear pre-secondary evaporation 4 is connected with a feed port of the second evaporator 5, a discharge port of the second evaporator 5 is connected with an inlet of the second evaporation pump P2, an outlet of the second evaporation pump P2 is connected with a feed port of the stripping tower 6, a bottom outlet of the stripping tower 6 is connected with an inlet of a stripping pump P3, the outlet of the stripping pump P3 is connected with the tube side inlet of the mixed oil heat exchanger 2, and the tube side outlet of the mixed oil heat exchanger 2 is connected with the mixed oil output tube G3.
The shell side steam inlet of the first evaporator 1 is connected with a gas phase pipe G2 of the desolventizer-toaster, a top steam outlet of the first evaporator 1 and a top steam outlet of the second evaporator 4 are connected with an inlet of the evaporative condenser 7, a steam outlet of the evaporative condenser 7 is connected with an injection port of the evaporative injection pump 10, and a mixed steam outlet of the evaporative injection pump 10 is connected with a shell side steam inlet of the second evaporator 4.
The top steam outlet of the second evaporator 5 and the top steam outlet of the stripping tower 6 are connected with the shell-side steam inlet of the front pre-secondary-steaming unit 3, the shell-side steam outlet of the front pre-secondary-steaming unit 3 is connected with the shell-side inlet of the stripping pre-condenser 8, the shell-side condensate outlet of the front pre-secondary-steaming unit 3 is connected with the water distribution box, the tube side of the stripping pre-condenser 8 is connected with a fresh solvent tube G4, the shell-side steam outlet of the stripping pre-condenser 8 is connected with the inlet of the stripping condenser 9, the shell-side steam outlet of the stripping condenser 9 is connected with the injection port of the stripping injection pump 11, and the mixed steam outlet of the stripping injection pump 11 is also connected with the shell-side steam inlet of the rear pre-secondary-steaming unit 4.
The first evaporator 1 utilizes the waste heat of the previous desolventizer-toaster as a heat source, the outlet of the mixed oil heat exchanger 2 is provided with the front pre-secondary evaporator 3, the mixed oil at the outlet of the mixed oil heat exchanger 2 is heated by utilizing the heat of the gas phase of the second evaporator 5 and the stripper 6, the temperature of the mixed oil can be increased by 5-10 ℃, and the steam consumption of the second evaporator 5 can be saved.
Outlets of the evaporation jet pump 10 and the stripping jet pump 11 are connected with a shell pass inlet of the post-secondary evaporation 4, mixed oil at the outlet of the post-secondary evaporation 4 is heated by using heat of mixed gas of the jet pumps, the temperature of the mixed oil is continuously increased by 5-15 ℃, and steam consumption of the second evaporator 5 can be further saved. The motive ports of the evaporation jet pump 10 and the stripping jet pump 11 are connected to a raw steam pipe G5.
The mixed gas at the gas phase outlet of the front-second-steaming 3 shell pass is used for heating the fresh solvent through the stripping pre-condenser 8, so that the steam consumption of the solvent heater can be saved, and the steam consumption can be reduced by 3-6kg per ton of oil.
The mixed oil with the concentration of 25-30% wt is sent into the first evaporator 1 from the mixed oil input pipe G1 to be evaporated, the first evaporator 1 heats the mixed oil to 55-60 ℃, and the concentration is increased to 75-85% wt; and then the first-steaming mixed oil is sent into a mixed oil heat exchanger 2 by a first-steaming extraction pump P1, the mixed oil is continuously heated by a first pre-second-steaming unit 3 after the oil temperature is increased to 70-75 ℃, the oil temperature is increased to 80-85 ℃, then the mixed oil is heated to 90-95 ℃ by a second pre-second-steaming unit 4, then the mixed oil enters a second evaporator 5 and is heated to 105-110 ℃ for evaporation, the concentration of the mixed oil is increased to 95-97 wt%, and finally the mixed oil enters a stripping tower 6, and the concentration is increased to more than 99.995 wt%.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments. All the technical solutions formed by adopting equivalent substitutions or equivalent transformations fall within the protection scope claimed by the present invention. The undescribed technical features of the present invention can be realized by or using the prior art, and are not described herein again.
Claims (3)
1. The utility model provides a miscella evaporation desolventizing system, includes the first evaporimeter that links to each other with the miscella input tube which characterized in that: the device comprises a first evaporator, a mixed oil heat exchanger and a steam extraction pump, wherein a discharge port of the first evaporator is connected with an inlet of the first steam extraction pump, an outlet of the first steam extraction pump is connected with a shell pass inlet of the mixed oil heat exchanger, a shell pass outlet of the mixed oil heat exchanger is connected with a feed port of the first steam extraction pump, a discharge port of the first steam extraction pump is connected with a feed port of the second steam extraction pump, an outlet of the second steam extraction pump is connected with a feed port of a stripping tower, a bottom outlet of the stripping tower is connected with an inlet of a stripping pump, an outlet of the stripping pump is connected with a tube pass inlet of the mixed oil heat exchanger, and a tube pass outlet of the mixed oil heat exchanger is connected with a mixed oil output tube.
2. The mixed oil evaporative desolventizing system according to claim 1, wherein: the shell side steam inlet of the first evaporator is connected with a gas phase pipe of the evaporator-evaporator machine, a top steam outlet of the first evaporator and a top steam outlet of the second-steam-preheating device are connected with an inlet of the evaporative condenser, a steam outlet of the evaporative condenser is connected with an injection port of the evaporative injection pump, and a mixed steam outlet of the evaporative injection pump is connected with the shell side steam inlet of the second-steam-preheating device.
3. The mixed oil evaporative desolventizing system according to claim 1 or 2, characterized in that: the top steam outlet of the second evaporator and the top steam outlet of the stripping tower are connected with the shell-side steam inlet of the pre-secondary steam, the shell-side steam outlet of the pre-secondary steam is connected with the shell-side inlet of a stripping pre-condenser, the shell-side condensate outlet of the pre-secondary steam is connected with a water distribution box, the tube side of the stripping pre-condenser is connected with a fresh solvent tube, the shell-side steam outlet of the stripping pre-condenser is connected with the inlet of the stripping condenser, the shell-side steam outlet of the stripping condenser is connected with the injection port of a stripping injection pump, and the mixed steam outlet of the stripping injection pump is also connected with the shell-side steam inlet of the post-secondary steam.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022813647.XU CN214088436U (en) | 2020-11-30 | 2020-11-30 | Mixed oil evaporation desolventizing system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202022813647.XU CN214088436U (en) | 2020-11-30 | 2020-11-30 | Mixed oil evaporation desolventizing system |
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| CN214088436U true CN214088436U (en) | 2021-08-31 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114470841A (en) * | 2022-03-15 | 2022-05-13 | 郑州良弓工程有限公司 | Heat energy recovery equipment for pre-dipping workshop section |
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