CN218089466U - Device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation - Google Patents
Device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation Download PDFInfo
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- CN218089466U CN218089466U CN202222435004.5U CN202222435004U CN218089466U CN 218089466 U CN218089466 U CN 218089466U CN 202222435004 U CN202222435004 U CN 202222435004U CN 218089466 U CN218089466 U CN 218089466U
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Abstract
The utility model relates to a low temperature desolventizing and miscella evaporation secondary steam's utilization device, including low temperature desolventizing unit, miscella evaporation unit, adopt the utility model discloses the device is evaporated in miscella evaporation technology one and is set up to climbing film evaporator negative pressure evaporation, and two evaporate and set up to falling film evaporator atmospheric pressure evaporation, and the vaporized secondary steam can be sent into low temperature desolventizing system heating material desolventizing as the heat source, then the secondary steam of low temperature desolventizing system is constituteed jointly with the secondary steam that the desolventizing produced to the secondary steam after the low temperature desolventizing back cooling, gets into a climbing film evaporator shell side as the heat source, has realized the secondary steam inter utilization of vaporization system and desolventizing system, and the secondary steam utilization ratio is higher, and energy-conservation is subtracted.
Description
Technical Field
The utility model relates to a grain and oil processing low temperature leaches technical field, concretely relates to low temperature desolventizing and miscella evaporation secondary steam's utilization device.
Background
The low-temperature desolventizing mode of the low-temperature leaching workshop is generally flash evaporation desolventizing of the cylinder A and the cylinder B, namely, circulating solvent steam is used as a heat carrier, the circulating solvent steam is heated to 125-135 ℃, the heated solvent steam is fully contacted with low-temperature meal containing the solvent in a desolventizing machine of the cylinder A to remove the solvent in the low-temperature meal by heating, the temperature of the circulating solvent steam is reduced, the circulating solvent steam and secondary steam generated by desolventizing are discharged out of the desolventizing machine of the cylinder A together, then the desolventizing secondary steam is discharged out of a low-temperature desolventizing system to remove steam as a heat source, the circulating solvent steam after being cooled is heated to 125-135 ℃ again, the desolventizing machine of the cylinder A is removed for recycling, and the low-temperature desolventizing system is the most main part of steam consumption of the workshop.
The evaporation process of the mixed oil in the low-temperature leaching workshop is generally divided into two types according to the evaporation pressure: normal pressure evaporation and negative pressure evaporation, wherein the normal pressure evaporation refers to that the first evaporation and the second evaporation are used for evaporating the solvent in the mixed oil under the normal pressure state; the negative pressure evaporation refers to that the first evaporation and the second evaporation are both used for evaporating the solvent in the mixed oil under the negative pressure state. In the traditional evaporation process, the structure selection of the evaporator is generally divided into two types, wherein the main selection type is that a first evaporation type and a second evaporation type are both climbing-film evaporators, the other selection type is that the first evaporation type is a falling-film evaporator, and the second evaporation type is the climbing-film evaporator. In the traditional evaporation process, no matter normal pressure evaporation or negative pressure evaporation is adopted, secondary steam is not utilized, and steam is greatly wasted. The mixed oil in the low-temperature leaching workshop is evaporated at normal pressure, and the first evaporation and the second evaporation are both evaporated at normal pressure, so that the solvent is not easy to evaporate due to high boiling temperature at normal pressure, only steam can be used as a heat source for evaporation, and the steam consumption is high; negative pressure evaporation, wherein the first evaporation and the second evaporation are evaporated in a negative pressure state, the vacuum degrees of the first evaporation and the second evaporation are generally the same, the vacuum degrees are-0.03 to-0.05 mpa, the first evaporation and the second evaporation adopt 1 vacuum pump, the vacuum pump generally adopts a steam jet pump, the boiling point of a solvent is reduced in the negative pressure state, the heat sources of the first evaporation generally comprise secondary steam of an evaporation system and steam of the steam jet pump of the evaporation system, the heat source of the second evaporation generally comprises steam, and the secondary steam of the first evaporation and the second evaporation directly enters a condenser for condensation; the evaporated secondary steam is not fully utilized, and energy waste is caused.
SUMMERY OF THE UTILITY MODEL
To the extravagant technical problem of heat source in the low temperature leaching treatment, the utility model provides a device of utilizing of low temperature desolventizing and miscella evaporation secondary steam can effectively utilize the heat of low temperature desolventizing and miscella evaporation secondary steam, has improved the utilization ratio of the energy, and energy-conservation subtracts the consumption.
The utility model provides a device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation, which comprises a low-temperature desolventizing unit and a mixed oil evaporation unit;
the low-temperature desolventizing unit comprises an A-cylinder desolventizing machine, a solvent vapor heater, a circulating fan and a first cyclone dust collector, wherein a vapor inlet of the A-cylinder desolventizing machine is connected with a vapor outlet of the solvent vapor heater through a pipeline, a vapor inlet of the solvent vapor heater is connected with an air outlet of the circulating fan through a pipeline, an air inlet of the circulating fan is connected with an outlet at the top of the first cyclone dust collector through a pipeline, and an inlet at the side part of the first cyclone dust collector is connected with the vapor outlet of the A-cylinder desolventizing machine through a pipeline;
the mixed oil evaporation unit comprises a second cyclone dust collector, a wet-type collector, a climbing-film evaporator, an evaporation flash box, a temporary storage tank, two evaporation feed pumps, two evaporation falling-film evaporators, two evaporation flash boxes and a high-pressure fan, wherein a side inlet of the second cyclone dust collector is connected with an air outlet of a circulating fan through a pipeline, a top outlet of the second cyclone dust collector is connected with a side inlet of the wet-type collector through a pipeline, a top outlet of the wet-type collector is connected with a side inlet of the evaporation film evaporator through a pipeline, a top outlet of the evaporation film evaporator is connected with a side inlet of the evaporation flash box through a pipeline, a bottom outlet of the evaporation flash box is connected with a top inlet of the temporary storage tank through a pipeline, a bottom outlet of the temporary storage tank is connected with a feed inlet of the two evaporation feed pumps through a pipeline, a discharge outlet of the two evaporation feed pumps is connected with a top feed inlet of the two evaporation falling-film evaporators through a pipeline, a side outlet of the evaporation flash box is connected with a side inlet of the evaporation flash box through a pipeline, a top outlet of the two evaporation flash box is connected with an air inlet of the high-pressure fan through a pipeline, and an air outlet of a steam heater is connected with an agent through a steam body input port of the high-pressure fan.
The device further comprises a condensation unit, the condensation unit comprises a first condenser, a second condenser and a water ring vacuum pump, an inlet of the first condenser is connected with an outlet at the top of the second evaporation flash tank and an outlet of a heat exchange medium at the side of the evaporation film evaporator through a pipeline, an inlet of the second condenser is connected with a steam outlet at the top of the evaporation flash tank through a pipeline, and the water ring vacuum pump is connected with an outlet of the second condenser.
Furthermore, the device also comprises a stripping feed pump, outlets at the bottoms of the secondary evaporation falling-film evaporator and the secondary evaporation flash tank are connected with a feed port of the stripping feed pump through a pipeline, and a discharge port of the stripping feed pump is connected with the stripping tower through a pipeline.
Furthermore, the outlet of the first condenser is also connected with the inlet of the second condenser through a pipeline.
Further, the A cylinder desolventizing machine is provided with a feeding port for feeding leached wet meal.
Furthermore, a mixed oil feeding device is arranged at the bottom of the evaporation climbing-film evaporator and comprises a mixed oil storage tank and a material pumping pump.
The beneficial effects of the utility model reside in that, the utility model discloses evaporate at the miscella evaporation one and set up to climbing film evaporation ware negative pressure evaporation, two evaporate and set up to falling film evaporation ware ordinary pressure evaporation, the flash steam of evaporation can be sent into low temperature desolventizing system heating material desolventizing as the heat source, then the flash steam of low temperature desolventizing system is constituteed jointly with the flash steam that desolventizing produced to flash steam after the low temperature desolventizing back cooling, get into a climbing film evaporation ware shell pass as the heat source, the flash steam mutually utilized of evaporation system and desolventizing system has been realized, the flash steam utilization ratio is higher, energy saving and loss reduction.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious for those skilled in the art to obtain other drawings without creative efforts.
Fig. 1 is a schematic structural diagram of embodiment 1 of the present invention.
In the figure, 1-a-evaporation climbing-film evaporator, 2-a-evaporation flash box, 3-a temporary storage tank, 4-a-evaporation feed pump, 5-a-evaporation falling-film evaporator, 6-a-evaporation flash box, 7-a stripping feed pump, 8-a second condenser, 9-a water ring vacuum pump, 10-a high pressure fan, 11-a solvent vapor heater, 12-a cylinder desolventizing machine, 13-a first cyclone dust collector, 14-a circulating fan, 15-a circulating solvent vapor control valve, 16-a low-temperature desolventizing secondary vapor control valve, 17-a second cyclone dust collector, 18-a wet type collector, 19-a first condenser, 20-a feeding port and 21-a mixed oil feeding device.
Detailed Description
In order to make the technical solutions of the present invention better understood by those skilled in the art, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, but not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by a person skilled in the art without creative efforts shall fall within the protection scope of the present invention.
Example 1
As shown in fig. 1, the device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporating of the present invention comprises a low-temperature desolventizing unit and a mixed oil evaporating unit;
the low-temperature desolventizing unit comprises an A-cylinder desolventizing machine 12, a solvent vapor heater 11, a circulating fan 14 and a first cyclone dust collector 13, wherein the A-cylinder desolventizing machine 12 is provided with a feeding port 20 for feeding leached wet meal, a vapor inlet of the A-cylinder desolventizing machine 12 is connected with a vapor outlet of the solvent vapor heater 11 through a pipeline, a vapor inlet of the solvent vapor heater 11 is connected with an air outlet of the circulating fan 14 through a pipeline, an air inlet of the circulating fan 14 is connected with an outlet at the top of the first cyclone dust collector 13 through a pipeline, and an inlet at the side part of the first cyclone dust collector 13 is connected with a vapor outlet of the A-cylinder desolventizing machine 12 through a pipeline;
the mixed oil evaporation unit comprises a second cyclone dust collector 17, a wet-type trap 18, a first evaporation-evaporation film evaporator 1, a first evaporation-flash box 2, a temporary storage tank 3, a second evaporation feed pump 4, a second evaporation-falling film evaporator 5, a second evaporation-flash box 6 and a high-pressure fan 10, wherein the inlet at the side part of the second cyclone dust collector 17 is connected with the air outlet of a circulating fan 14 through a pipeline, the outlet at the top part of the second cyclone dust collector 17 is connected with the inlet at the side part of the wet-type trap 18 through a pipeline, the outlet at the top part of the wet-type trap 18 is connected with the inlet at the side part of the first evaporation-flash box 1 through a pipeline, the outlet at the top part of the first evaporation-flash box 1 is connected with the inlet at the side part of the first evaporation-flash box 2 through a pipeline, the outlet at the bottom part of the first evaporation-flash box 2 is connected with the inlet at the top part of the temporary storage tank 3 through a pipeline, the outlet at the bottom part of the temporary storage tank 3 is connected with the inlet of the second evaporation-flash pump 4 through a pipeline, the discharge port of the second evaporation-flash box 4 is connected with the inlet at the top part of the second evaporation-falling film evaporator 5 through a pipeline, the inlet through a pipeline, the outlet of the second evaporation-flash box 5 is connected with the inlet of the high-flash box 10 through a pipeline, and the high-flash box 11 through a high-pressure fan through a pipeline, and the high-flash box 11;
still include the condensing unit, the condensing unit includes first condenser 19, second condenser 8, water ring vacuum pump 9, and the first condenser 19 entry is through pipe connection two evaporation flash tank 6 top exports and the export of 1 lateral part heat transfer medium of a evaporation climbing film evaporator, and the export of 2 top steam body of a evaporation flash tank is passed through the pipe connection to the second condenser 8 entry, and the export of water ring vacuum pump 9 connection second condenser 8 still passes through the pipe connection second condenser 8 entry.
The outlets at the bottoms of the two-evaporation falling-film evaporator 5 and the two-evaporation flash tank 6 are also connected with the feed inlet of a stripping feed pump 7 through a pipeline, the discharge outlet of the stripping feed pump 7 is connected with a stripping tower through a pipeline, and the separated mixed oil is sent to the stripping tower for stripping.
The method for utilizing the device for low-temperature desolventizing and mixed oil evaporation secondary steam comprises the following steps:
s1, heating solvent vapor in a solvent vapor heater 11 and sending the heated solvent vapor to a desolventizing machine A12, contacting the heated solvent vapor with low-temperature meal containing a solvent, heating the low-temperature meal to remove the solvent, setting the heating temperature in the solvent vapor heater 11 to be 130 ℃, and setting the pressure to be-1.5 KPa;
s2, after heat exchange and temperature reduction, mixed gas of the solvent vapor at 85 ℃ and desolventizing secondary steam enters a circulating fan 14 after being dedusted by a first cyclone deduster 13; adjusting a circulating solvent vapor control valve 15 and a low-temperature desolventizing secondary vapor control valve 16, returning a part of mixed vapor to a solvent vapor heater 11 by a circulating fan 14 for repeated heating and use, and sending the rest mixed vapor to a second cyclone dust collector 17;
s3, the mixed gas with dust removed by the second cyclone dust collector 17 and the wet trap 18 enters a shell pass of a rising evaporation film evaporator 1 to serve as a heat source to heat the mixed oil, then the non-condensable gas enters a first condenser 19 to be condensed again and then enters a tail gas absorption system, negative pressure evaporation is carried out in the rising evaporation film evaporator 1, a water ring vacuum pump 9 is adjusted to enable the vacuum degree of the negative pressure evaporation to be-0.060 MPa, the evaporated mixed oil enters a flash evaporation box 2 to be separated, the separated mixed oil enters a temporary storage tank 3, steam generated by the flash evaporation box 2 enters a second condenser 8, and the non-condensable gas generated after condensation enters the tail gas absorption system through the water ring vacuum pump 9;
s4, quantitatively feeding the mixed oil in the temporary storage tank 3 into a secondary evaporation falling-film evaporator 5 by a secondary evaporation feed pump 4 for evaporation, adjusting the frequency of a high-pressure fan 10 to enable the pressure of the secondary evaporation falling-film evaporator 5 and the secondary evaporation flash tank 6 to be-2 kpa, feeding the evaporated mixed oil into the secondary evaporation flash tank 6 for separation, adjusting the opening of a secondary evaporation valve according to the temperature of the mixed oil at the outlet of the secondary evaporation flash tank 6 to enable the temperature of the mixed oil to be 120 ℃, and simultaneously feeding secondary steam evaporated under the action of the high-pressure fan 10 into a solvent steam heater 11 in the step S1 to be mixed and heated with solvent steam.
Although the present invention has been described in detail by referring to the drawings in conjunction with the preferred embodiments, the present invention is not limited thereto. Various equivalent modifications or substitutions can be made on the embodiments of the present invention by those skilled in the art without departing from the spirit and substance of the present invention, and these modifications or substitutions are intended to be within the scope of the present invention/any person skilled in the art can easily conceive of changes or substitutions within the technical scope of the present invention.
Claims (6)
1. A device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation is characterized by comprising a low-temperature desolventizing unit and a mixed oil evaporation unit;
the low-temperature desolventizing unit comprises an A-cylinder desolventizing machine, a solvent vapor heater, a circulating fan and a first cyclone dust collector, wherein a vapor inlet of the A-cylinder desolventizing machine is connected with a vapor outlet of the solvent vapor heater through a pipeline, a vapor inlet of the solvent vapor heater is connected with an air outlet of the circulating fan through a pipeline, an air inlet of the circulating fan is connected with an outlet at the top of the first cyclone dust collector through a pipeline, and an inlet at the side part of the first cyclone dust collector is connected with the vapor outlet of the A-cylinder desolventizing machine through a pipeline;
the mixed oil evaporation unit comprises a second cyclone dust collector, a wet-type collector, an evaporation film evaporator, an evaporation flash box, a temporary storage tank, two evaporation feed pumps, two evaporation falling film evaporators, two evaporation flash boxes and a high-pressure fan, wherein a side inlet of the second cyclone dust collector is connected with an air outlet of a circulating fan through a pipeline, a top outlet of the second cyclone dust collector is connected with a side inlet of the wet-type collector through a pipeline, a top outlet of the wet-type collector is connected with a side inlet of the evaporation film evaporator through a pipeline, a top outlet of the evaporation film evaporator is connected with a side inlet of the evaporation flash box through a pipeline, a bottom outlet of the evaporation flash box is connected with a top inlet of the temporary storage tank through a pipeline, a bottom outlet of the temporary storage tank is connected with a feed inlet of the second evaporation feed pump through a pipeline, a discharge outlet of the second evaporation feed pump is connected with a top feed inlet of the second evaporation falling film evaporator through a pipeline, a side outlet of the evaporation falling film evaporator is connected with a side inlet of the evaporation flash box through a pipeline, a top outlet of the second evaporation flash box is connected with a high-pressure fan through a pipeline, and an air outlet of the high-pressure fan is connected with a steam body heater through a pipeline.
2. The device for utilizing the secondary steam generated by the evaporation of the low-temperature desolventizing and mixed oil as claimed in claim 1, further comprising a condensing unit, wherein the condensing unit comprises a first condenser, a second condenser and a water ring vacuum pump, an inlet of the first condenser is connected with a top outlet of the two evaporation flash tanks and a side heat exchange medium outlet of the evaporation lift membrane evaporator through pipelines, an inlet of the second condenser is connected with a top steam outlet of the evaporation flash tanks through pipelines, and the water ring vacuum pump is connected with an outlet of the second condenser.
3. The device for utilizing the secondary steam generated by the low-temperature desolventizing and the mixed oil evaporation as claimed in claim 1, further comprising a stripping feed pump, wherein the outlets at the bottoms of the two-evaporation falling-film evaporator and the two-evaporation flash tank are connected with the feed port of the stripping feed pump through pipelines, and the discharge port of the stripping feed pump is connected with the stripping tower through a pipeline.
4. The apparatus for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporating as claimed in claim 2, wherein the outlet of the first condenser is further connected to the inlet of the second condenser through a pipeline.
5. The apparatus for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation as claimed in claim 1, wherein the A-barrel desolventizing machine is provided with a feeding port for feeding leached wet meal.
6. The apparatus for utilizing secondary steam in low-temperature desolventizing and mixed oil evaporation as claimed in claim 1, wherein a mixed oil feeding device is provided at the bottom of a distillation-rising film evaporator.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222435004.5U CN218089466U (en) | 2022-09-14 | 2022-09-14 | Device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222435004.5U CN218089466U (en) | 2022-09-14 | 2022-09-14 | Device for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
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