CN103865636A - Leaching process of semi-negative pressure vacuum system - Google Patents
Leaching process of semi-negative pressure vacuum system Download PDFInfo
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- CN103865636A CN103865636A CN201210562439.4A CN201210562439A CN103865636A CN 103865636 A CN103865636 A CN 103865636A CN 201210562439 A CN201210562439 A CN 201210562439A CN 103865636 A CN103865636 A CN 103865636A
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Abstract
The invention discloses a leaching process of a semi-negative pressure vacuum system. The evaporation temperature is reduced by utilizing the situation that the boiling point of mixed oil is reduced in a negative pressure state; a vacuum environment is set through local equipment to achieve an energy-saving effect. A long evaporator is vacuumized by arranging a steam injection vacuum pump and a water ring type vacuum pump; the evaporation temperature of solvent oil is reduced. Solvent mixed gas of an evapo-separated machine is drawn by the steam injection vacuum pump and the water ring type vacuum pump, and solvent recovery is performed after the solvent mixed gas enters an energy saver. The secondary steam temperature of the evapo-separated machine is 80-82 DEG C, secondary steam of the evapo-separated machine and steam injected from the steam injection pump are taken as heating steam of a shell side of the long evaporator, and then the secondary steam of the evapo-separated machine can be effectively utilized for heating the long evaporator. Thus, the secondary steam of the evapo-separated machine and the secondary steam injected from the steam injection pump can be effectively utilized to achieve the energy-saving effect.
Description
Technical field:
Technique of the present invention, is applied to food oils and soaks oil plant by solvent oil; Make lubricant component in oil plant be melted to then separation, cooling in solvent oil; Recovered solvent oil is also isolated the technical field that eats crude oil.
Background technology:
Each large and medium-sized grease company produces most of extract technology that adopts at grease.Adopt solvent oil (No. six petroleum naphthas) glyceride stock to be carried out after abundant immersion to high temperature extraction, maximum feature is that oil yield is high, production cost is low.Along with the aggravation of the international progress of trade and competition, the mass-producing of domestic grease processing enterprise, automated process are accelerated rapidly, and some large-scale modernization Oils and fats enterprises build up at home in succession, and the current oil prodution industry level of China is by leaps and bounds improved.Because small scale, state of the art fall behind, be all faced with at present technological transformation and strategical adjustment.How to make rational use of resources, reduce production costs, expand the scale of production, improve enterprise technology and level of management, improve competitiveness, become the target that more multiple enterprises is pursued.The key of grease production, the number of its energy consumption, molten consumption will directly have influence on the production cost of grease processing enterprise.Current small-scale grease company extract technology is all to adopt conventional extract technology-normal pressure extract technology, and this process solvent oil vapour point is higher, uses quantity of steam larger; Consume energy high, the residual molten rate of dregs of rice material is high, causes edible oil cost high.The general trend of market development is higher to special oil parent degree of looking at, and the oil plant of special oil comparatively disperses; Therefore the applicable special oil of producing of small-scale grease company.The related technique of this project, can address the above problem.
Summary of the invention:
Technique of the present invention, utilizes under negative pressure state, mixing oil boiling point lowering, thus reduce vaporization temperature; By local devices, vacuum environment is set and reaches energy-conservation effect.By steam jet vacuum pump and water-ring vacuum pump are set, a long vaporizer is evacuated; The vaporization temperature of solvent oil is reduced.Steam jet vacuum pump and water-ring vacuum pump extract the solvent gas of evapo-separated machine, carry out solvent recuperation after entering energy-saving appliance.According to the secondary steam temperature of evapo-separated machine at 80-82 ℃, the steam spraying using the secondary steam of evapo-separated machine with from vapor jet pump is as the heating steam of the shell side of a long vaporizer, and the secondary steam that just can effectively utilize evapo-separated machine heats a long vaporizer.To effectively utilize and reach energy-conservation effect by the secondary steam of evapo-separated machine with from the secondary steam of vapor jet pump ejection like this.
Accompanying drawing explanation:
Below in conjunction with drawings and Examples, the present invention is further described, and Fig. 1 is the process principle figure of half negative-pressure vacuum system extract technology.
System is by the flat scraper plate 1 of charging, bury scraper plate 2 No. one, feeding spiral conveyer 3, leacher 4, solvent Impulsive tank 5, bury scraper plate 6 No. two, evapo-separated machine 7, discharging spiral conveyor 8, wastewater boilling tank 9, salt water tank 10, the tank 11 of saltouing, miscella tank 12, one long vaporizer 13, two long vaporizers 14, swash plate stripping tower 15, crude oil tank 16, steam de-condenser 17, diversion box 18, one long condenser 19, two long condensers 20, solvent tank 21, circulating water pool 22, counter-flow cooling tower 23, miscella filter 24, solvent heater 25, combination trap 26, spray trap 27, steam jet vacuum pump 28, one steams separator 29, leach condenser 30, water ring vacuum pump 31, energy-saving appliance 32, surge tank 33, solvent condenser 34, exhaust fan 35, tail gas absorber 36, last condenser 37, air lift condenser 38.
Embodiment:
Technique of the present invention, oil plant is transported to and is provided with buffer bin through charging scraper plate 1 as shown in Figure 1; Oil plant is transported to feeding spiral conveyer 3 entering below buffer bin and burying scraper plate 2 for No. one.Be transported to leacher 4 and leach operation; Solvent oil is transported to solvent Impulsive tank 5 after 2 heating of solvent oil well heater, and solvent Impulsive tank 5 carries out timing according to leacher 4 processing requirements provides solvent oil; Oil plant extracts food oils after soaking by solvent oil setting-up time to be mixed with solvent oil.Mixing oil repeats to leach through several times, and the food oils in mixing oil reach after optimum concn; Mixing crude oil is input to miscella filter 24 through oil pump and filters.After hybrid oil filter, be transported to the tank 11 of saltouing, the tank top of saltouing is provided with salt water tank 10 provides salt solution; The tank 11 that makes to saltout mixes well cuts and separates out postprecipitation and discharge through evacuation port.It is temporary that mixing oil enters miscella tank 12, and in the time that liquid level reaches certain altitude, oil pump pumps into that a long vaporizer 13 is interior evaporate separation to the solvent oil in mixing oil and eat crude oil; Steam separator 29 and produce vacuum owing to being provided with the long vaporizer of steam jet vacuum pump 28, water ring vacuum pump 31, one 13; The vapour point of solvent oil is reduced.The long vaporizer 13 of Secondary-steam heating one of steam jet vacuum pump 28 and evapo-separated machine 7, makes the solvent oil evaporation in long vaporizer 13 mixing oils, after separating by a steaming separator 29; Mixing oil enters two long vaporizers 14 and again evaporates.After separating, mixing oil enters swash plate stripping tower 15 and carries out last stripping evaporating solvent oil; Mixing oil input enters in crude oil tank 16 temporary, is input in crude oil storehouse and stores when liquid level reaches certain liquid level.The wet dregs of rice of oil plant from leacher 4 soaks by burying scraper plate 6 No. two, steam de-hermetic conveyer and enter evapo-separated machine 7, solvent oil in the wet oil plant dregs of rice is steamed and is taken off; The dry dregs of rice store in discharging spiral conveyor 8 is inputted dregs of rice storehouse.The gaseous solvent oil evaporating at evapo-separated machine 7, through combination trap 26, spray trap 27, steams de-condenser 17 by entering after dregs of rice trapping; After condensation, changing into liquid solvent oil is input to diversion box 18 and reclaims.Enter a long condenser 19 from the gaseous solvent oil of a steaming separator 29, after condensation, change into liquid solvent oil and be input to diversion box 18 and reclaim; The gaseous solvent oil evaporating from swash plate stripping tower 15 enters and changes into liquid solvent oil 38 condensations of air lift condenser and be input to diversion box 18 and reclaim.Mixed solution in diversion box 18 enters wastewater boilling tank 9 and heats, and makes liquid solvent oil become gaseous solvent oil cooling and carries out solvent oil circulation after solidifying and reclaim.The bottom that enters tail gas absorber 36 from condenser free gas out, waste gas is discharged in atmospheric layer by exhaust fan 35.So also make leaching system produce certain negative pressure, be conducive to evaporate in system, loss is emitted in the race of condensing equipment solvent.Solvent gas enters last condenser 37, and the liquid of condensation enters diversion box 18 and processes.
Claims (5)
1. a half negative-pressure vacuum system extract technology, its feature: steam jet vacuum pump and water-ring vacuum pump are set, a long vaporizer is evacuated; The vaporization temperature of solvent oil is reduced.According to the secondary steam temperature of evapo-separated machine, at 80-82 ℃, the steam spraying using the secondary steam of evapo-separated machine with from vapor jet pump is as the heating steam of the shell side of a long vaporizer, and the secondary steam that effectively utilizes evapo-separated machine heats a long vaporizer.
2. technique according to claim 1, oil plant is transported to and is provided with buffer bin through charging scraper plate (1); Oil plant enters from buffer bin below to bury for No. one and is transported to feeding spiral conveyer (3) scraper plate (2) and is transported to leacher 4 and leaches operation.
3. technique according to claim 1, solvent oil is transported to solvent Impulsive tank (5) after solvent oil well heater (2) heating, and solvent tank requires to carry out timing according to extract technology solvent oil is provided; Oil plant extracts food oils after soaking by solvent oil setting-up time to be mixed with solvent oil.
4. technique according to claim 1, mixing crude oil is input to miscella filter (24) through oil pump and filters.After hybrid oil filter, be transported to the tank of saltouing (11), the tank top of saltouing is provided with salt water tank (10) provides salt solution; The tank mixing well cuts that makes to saltout is separated out postprecipitation and is discharged through evacuation port.
5. technique according to claim 1, is provided with steam jet vacuum pump (28), water ring vacuum pump (31) generation vacuum; The vapour point of solvent oil is reduced.The long vaporizer of Secondary-steam heating one (13) of steam jet vacuum pump (28) and evapo-separated machine (7), makes the solvent oil evaporation in mixing oil.After separating by a steaming separator (29); Mixing oil enters two long vaporizers (14) and again evaporates.After separating, mixing oil enters swash plate stripping tower (15) and carries out last stripping evaporating solvent oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210562439.4A CN103865636A (en) | 2012-12-17 | 2012-12-17 | Leaching process of semi-negative pressure vacuum system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210562439.4A CN103865636A (en) | 2012-12-17 | 2012-12-17 | Leaching process of semi-negative pressure vacuum system |
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| CN103865636A true CN103865636A (en) | 2014-06-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201210562439.4A Pending CN103865636A (en) | 2012-12-17 | 2012-12-17 | Leaching process of semi-negative pressure vacuum system |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111471519A (en) * | 2020-05-14 | 2020-07-31 | 赵汇川 | Device and method for extracting cashew nut shell oil |
| CN111944606A (en) * | 2019-05-17 | 2020-11-17 | 清馨(北京)科技有限公司 | Novel evaporation system |
| CN112048382A (en) * | 2020-09-16 | 2020-12-08 | 湖南一代伟仁科技有限公司 | Method for improving quality of tea oil leaching and reducing energy consumption |
| CN115287121A (en) * | 2022-09-14 | 2022-11-04 | 山东凯斯达机械制造有限公司 | Method for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
-
2012
- 2012-12-17 CN CN201210562439.4A patent/CN103865636A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111944606A (en) * | 2019-05-17 | 2020-11-17 | 清馨(北京)科技有限公司 | Novel evaporation system |
| CN111471519A (en) * | 2020-05-14 | 2020-07-31 | 赵汇川 | Device and method for extracting cashew nut shell oil |
| CN112048382A (en) * | 2020-09-16 | 2020-12-08 | 湖南一代伟仁科技有限公司 | Method for improving quality of tea oil leaching and reducing energy consumption |
| CN115287121A (en) * | 2022-09-14 | 2022-11-04 | 山东凯斯达机械制造有限公司 | Method for utilizing secondary steam generated by low-temperature desolventizing and mixed oil evaporation |
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Application publication date: 20140618 |