CN104928024B - The depickling of high valent acid vegetable oil and fraction recovery method - Google Patents
The depickling of high valent acid vegetable oil and fraction recovery method Download PDFInfo
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- CN104928024B CN104928024B CN201510321598.9A CN201510321598A CN104928024B CN 104928024 B CN104928024 B CN 104928024B CN 201510321598 A CN201510321598 A CN 201510321598A CN 104928024 B CN104928024 B CN 104928024B
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Abstract
The present invention relates to a kind of depickling of high valent acid vegetable oil and fraction recovery methods, in turn include the following steps：Feedstock oil carries out indirect heat exchange after vacuum outgas with high temperature depickling oil, then carries out first order heating distillation and second level heating distillation successively, becomes high temperature depickling oil after two-step heating distillation；The low boiler cut steam that first order heating distillation generates enters after condensation recovering device is condensed into liquid, into low boiler cut storage tank；The high boiling fraction steam that second level heating distillation generates enters after condensation recovering device is condensed into liquid, into high boiling fraction storage tank；The fatty acid vapor of residue not being condensed in fraction, into aliphatic acid trap, is trapped by low temperature fatty acid liquid circulated sprinkling；The top of aliphatic acid trap is connected with pumped vacuum systems.This method meets the finished product acid value requirement of high valent acid vegetable oil, and deacidification neutral oil loss is few, and low boiling point and high boiling fraction can realize classification recycling, reduce the investment of subsequent purification.
Description
Technical field
The present invention relates to a kind of depickling of high valent acid vegetable oil and fraction recovery methods, belong to vegetable oil processing technology neck
Domain.
Background technology
Depickling is very important link in vegetable oil fine sweetening process, deacidifying device quality determine deacidifying process into
It loses.The method of the physical deacidification of the high valent acid vegetable oil carried out using high temperature high vacuum by steam distillation principle, without logical
The chemical deacidification for adding alkali is crossed, waste water is not generated, is conducive to environmental protection, greatly improve product（Oil）Yield, and height can be obtained
The acid byproduct fatty of added value.
In recent years, ordered structure filler is so that its is simple in structure, steam utilization is efficient, and it is excellent that the gas-liquid specific area provided is big etc.
Point be promoted rapidly, at present most of production lines use filler extracting tower, for the grease of high acid value, it is necessary to
Overhead oil entrance obtains very high oil temperature and provides all aliphatic acid evaporations required heat, and excessively high oil temperature can cause grease
Polymerization is decomposed, trans-fatty acid increase, if turning down oil inlet temperature, packed tower middle and lower part is reduced due to oil temperature under deacidification effect
Drop, depickling are not thorough.Secondly the oil product of high acid value is easily flashed in tower top high oil temperature, and significant quantities of fat acid vapor can cause neutral oil
Entrainment, product loss, it is not high to distill out acid byproduct fatty purity；In addition the filler floor height needed for the oil product depickling of high acid value
Depickling, the deodorization of the more general oil product of degree are high, the pressure drop that excessively high packing layer is brought so that bottom column bottom vacuum degree declines, and takes off
Sour ability reduces, and bottom of towe depickling oleic acid value is difficult to meet technological requirement.
For distilling out for fatty acid recovery, the fatty acid liquid of single-stage filler trap low temperature is generally used at present
Spray distills out fatty acid vapor to trap, the obtained separating-purifying for being fatty acid mixed, increasing follow-up acid byproduct fatty
Investment.
The content of the invention
It is an object of the present invention to overcome problems of the prior art, a kind of depickling of high valent acid vegetable oil is provided
And fraction recovery method, deacidification effect meet technological requirement, while to the low boiler cut and higher boiling in high valent acid vegetable oil
Fraction carries out classification recycling.
For solution more than technical problem, a kind of depickling of high valent acid vegetable oil of the invention and fraction recovery method, successively
Include the following steps：Feedstock oil, which enters in vacuum material tank, to be sprayed, and removes the moisture and air dissolved in feedstock oil, then
Feedstock oil and high temperature depickling oil carry out indirect heat exchange, are entered back into after feedstock oil heating in secondary distillation tower and carry out the first order successively and add
Thermal distillation and second level heating distillation, become high temperature depickling oil after two-step heating distillation, high temperature depickling oil with it is described
Enter depickling oil tank after feedstock oil indirect heat exchange；The low boiler cut steam that first order heating distillation generates is from low boiler cut
Steam inlet enters condensation recovering device and is cooled water indirect condensing into after liquid, into low boiler cut storage tank；It heats the second level
Distill generate high boiling fraction steam from high boiling fraction steam inlet enter condensation recovering device be cooled water indirect condensing into
After liquid, into high boiling fraction storage tank；The fatty acid vapor of residue not being condensed in fraction, from returning for condensation recovering device top
It receives device venthole and escapes and enter aliphatic acid trap, in the aliphatic acid trap, low temperature fatty acid liquid is to aliphatic acid
Steam carries out circulated sprinkling trapping, falls into the fatty acid liquid of aliphatic acid trap bottom, after being pumped out by aliphatic acid, through cooling
Water is returned at the top of the aliphatic acid trap after cooling down indirectly and sprayed；The top of the aliphatic acid trap is with vacuumizing
System is connected.
Compared with the prior art, the present invention achieves following advantageous effect：Pumped vacuum systems passes through head tank vacuum orifice
Carrying out suction makes the inner cavity of vacuum material tank be in vacuum state, and the high valent acid vegetable oil that preceding working procedure is come enters through raw material oil pipe
Head tank spray tube is sprayed, and due to distributing for nozzle, the moisture dissolved in vegetable oil, oxygen, air is removed totally, kept away
Exempt from mentioned component to have a negative impact to oil product in high temperature depickling；Vegetable oil after vacuum outgas is from vacuum material tank bottom
The head tank oil outlet outflow in portion, the depickling oil that vegetable oil heat exchanger and high temperature are pumped by crude oil carry out indirect heat exchange, depickling
The oil temperature of oil declines, the oil temperature rise of feedstock oil, and then feedstock oil is flowed out from the material oil outlet of plant oil heat exchanger, into two
The destilling tower oil inlet pipe of grade destilling tower, vegetable oil is by gradient-heated at twice in secondary distillation tower, but obtains Gao Zhen unanimous between the higher and lower levels
Reciprocal of duty cycle.The temperature of first order heating is slightly lower, and slightly lower vapo(u)rizing temperature realizes low boiler cut such as low-carbon chain fatty acid from oil
Volatilization is overflowed, and has boiling point difference using components such as aliphatic acid, low boiler cut preferentially removes in oil, from the top of secondary distillation tower
End vapors outlet discharge enters condensation recovering device condensation from low boiler cut steam inlet.Oil after level-one distillation is through two level
Reach higher vapo(u)rizing temperature after heating, ensure that the acid value of depickling oil requires, secondary distillation is by high boiling fraction such as high carbon chain
Fatty acid distillation goes out, and high boiling fraction enters from the middle part end vapors outlet discharge of secondary distillation tower from high boiling fraction steam
Mouth is condensed into condensation recovering device.Fractional distillation and recycling shorten vegetable oil through high temperature distillation while enhancing deacidification effect
Time, be conducive to the nutritional ingredients such as VE in oil, phytosterol, oryzanol reservation.Depickling oil after two level depickling is from two level
The destilling tower oil outlet outflow of tower bottom is distilled, the depickling oil inlet of plant oil heat exchanger is pumped by depickling oil pump, to feedstock oil
After being preheated, depickling oil is flowed out from the depickling oil export of plant oil heat exchanger, into depickling oil tank.Both depickling oil had been recycled
Heat, reduce the temperature of depickling oil, and preheated feedstock oil, reduce energy consumption.
As the preferred embodiment of the present invention, the temperature of the feedstock oil is 100 ± 5 DEG C, with being risen after high temperature depickling oil heat exchange
Temperature is to 190 ± 5 DEG C, and oil temperature rises to 220 ± 5 DEG C after the first order heats, and oil temperature rises to 240 ± 5 DEG C after the second level is heated, institute
The temperature stated before the oily heat exchange with the feedstock oil of high temperature depickling is 225 ± 5 DEG C, and the temperature after heat exchange is 135 ± 5 DEG C；Described two
The low boiler cut vapor (steam) temperature of grade destilling tower discharge is 115 ± 5 DEG C, the high boiling fraction steam of the secondary distillation tower discharge
Temperature is 125 ± 5 DEG C；The remaining aliphatic acid vapor (steam) temperature discharged from the condensation recovering device is 80 DEG C, the aliphatic acid trapping
In device, the spray temperature of low temperature fatty acid liquid is 50 DEG C；Absolute pressure in the aliphatic acid trap is 1.5mbar, institute
It is equal to state the absolute pressure that the first order heating distillation in vacuum material tank and the secondary distillation tower and second level heating are distilled
For 2mbar.
As the preferred embodiment of the present invention, the inner cavity top of the vacuum material tank is equipped with head tank spray tube, described true
Head tank vacuum orifice at the top of empty head tank is connected with the pumped vacuum systems, and the outlet of raw material oil pipe is sprayed with the head tank
The entrance of shower pipe is connected, and the head tank oil outlet of the vacuum material pot bottom and the entrance of crude oil pump connect, the crude oil pump
Outlet be connected with the raw material oil inlet of plant oil heat exchanger, the material oil outlet of the plant oil heat exchanger and secondary distillation tower
Destilling tower oil inlet pipe entrance connection, the destilling tower oil outlet of the secondary distillation tower bottom changes through depickling oil pump with vegetable oil
The depickling oil inlet connection of hot device, the depickling oil export of the plant oil heat exchanger are connected with depickling oil tank；The two level
The overhead fraction steam (vapor) outlet of destilling tower is connected with the low boiler cut steam inlet of the condensation recovering device, the secondary distillation
The middle part end vapors outlet of tower is connected with the high boiling fraction steam inlet of the condensation recovering device, the condensation recovering device
Recover venthole is connected with the pumped vacuum systems.
As the preferred embodiment of the present invention, the overhead fraction steam (vapor) outlet is located in the top of the secondary distillation tower
The heart, the overhead fraction steam (vapor) outlet are arranged right below top oil removing foam device, are set below the top oil removing foam device
There is top heating tank, the top heating tank is fixed on the inner wall circumference of the secondary distillation tower and open top, the steaming
The outlet for evaporating tower oil inlet pipe is inserted into below the pasta of the top heating tank, be equipped in the top heating tank upper portion heater and
Top overflow pipe, the bottom of the top heating tank are equipped with top and stir steam pipe, and the lower end of the top overflow pipe passes through institute
It states the bottom wall of top heating tank and is connected with the entrance of top oil dispenser, the lower section of the top oil dispenser is equipped with upper filler
Layer；The lower section of the upper packing layer is equipped with the oil-collecting annular groove being fixed on the secondary distillation inner wall of tower, the oil-collecting annular groove
Gear liquid cover is equipped with above centre bore；The bottom of the oil-collecting annular groove is connected with oil-collecting annular groove flowline, and the oil-collecting annular groove is fuel-displaced
Below the pasta of the lower end insertion middle part heating tank of pipe, middle part heater and middle part overflow pipe are equipped in the middle part heating tank,
The bottom of the middle part heating tank is equipped with middle part and stirs steam pipe, and the lower end of the middle part overflow pipe passes through the middle part heating tank
Bottom wall and insertion middle part oil pooling dipper pasta below, the outlet of the middle part oil pooling dipper and the entrance phase of middle part oil dispenser
Even, the lower section of the middle part oil dispenser is equipped with lower packing layer；It is equipped between the middle part oil pooling dipper and the middle part heating tank
Middle part oil removing foam device, middle part end vapors outlet be located at the middle part oil removing foam device and the middle part heating tank it
Between；The bottom of the secondary distillation tower is equipped with bottom and stirs steam pipe.Vegetable oil after vacuum outgas is from secondary distillation tower
Destilling tower oil inlet pipe enter in the heating tank of top, the multiple baffling in the heating tank of top, and be subject to top stirring steam pipe spray
The strong stirring for the live (open) steam penetrated, under the heating of upper portion heater, oil temperature is overflow after being increased to setting technological temperature from top
Flow tube to underflow stream flow out, through top oil dispenser distribution after uniformly spread in upper packing layer, in upper packing layer with middle part
Stirring steam in heating tank carries out full regression gas-liquid contact, the low boiler cut in vegetable oil under water vapor acting constantly
It evaporates, under the suction of vacuum power source, low boiler cut steam flows upward, by top oil removing foam device foam removal
Afterwards, flowed out from the overhead fraction steam (vapor) outlet at secondary distillation top of tower center；The vegetable oil distilled through level-one is spilt from upper packing layer
It falls into oil-collecting annular groove, then is flowed into from oil-collecting annular groove flowline in the heating tank of middle part, the multiple baffling in the heating tank of middle part after going out,
And it is subject to the strong stirring of the live (open) steam of middle part stirring steam pipe inspection, under the heating of middle part heater, oil temperature is after of continuing rising
Overflow pipe enters middle part oil pooling dipper to underflow stream in the middle part of Gao Houcong；Middle part oil pooling dipper is between the top of secondary distillation tower and middle part
Play the role of fluid-tight, vegetable oil is after the outflow of middle part oil pooling dipper, and uniform spread is in lower filler after the distribution of middle part oil dispenser
In layer, the stirring steam with bottom stirring steam pipe inspection in lower packing layer carries out full regression gas-liquid contact, in vegetable oil
High boiling fraction constantly evaporated under water vapor acting, under the suction of vacuum power source, high boiling fraction steam to
Upper flowing, after middle part oil removing foam device foam removal, from the middle part end vapors outlet outflow of secondary distillation tower.Through secondary distillation
Vegetable oil afterwards falls into the bottom of secondary distillation tower, is flowed out from destilling tower oil outlet.
As the further preferred embodiment of the present invention, the top oil removing foam device and the middle part oil removing foam device top
More folding waveform liquid barriers are respectively equipped on the ventilation section at center, the lower end periphery of more folding waveform liquid barriers is connected to
Annular catch tray, the excircle of the ring-type catch tray are tilted down and are connected on the inner wall of the secondary distillation tower；Each institute
The lower edge for stating more folding waveform liquid barriers is respectively equipped with the drop collection item that drop is oriented to the annular catch tray, the annular collection
The lowest part of liquid disk is respectively equipped with outage.Low boiler cut steam flows through more folding waveform liquid barriers of top oil removing foam device
When, when high boiling fraction steam flows through more folding waveform liquid barriers of middle part oil removing foam device, drop is blocked respectively, passes through drop
It collects item and flows into annular catch tray, then flowed downward out from the outage of annular catch tray lowest part along the barrel of secondary distillation tower.
As the further preferred embodiment of the present invention, upper wall is equipped with below the annular catch tray of the top oil removing foam device
Stream collects ring, and mesospore stream is equipped between the top heating tank and the top oil dispenser and collects ring, the upper wall stream
The lowest part for collecting ring is connected with diversion pipe, and mesospore stream described in the lower end aligned of the diversion pipe collects ring；The middle part
Lower wall stream is equipped with below the annular catch tray of oil removing foam device and collects ring, the mesospore stream collects ring and the lower wall stream is received
The lowest part of collection ring is respectively equipped with condensation fluid outlet, and the external end head of the condensation fluid outlet stretches out the two level and steams respectively
It evaporates outside the cylinder of tower and is connected respectively with condensate collector tube, the outlet of the condensate collector tube and entering for condensate liquid inlet valve
Mouth is connected, and the outlet of the condensate liquid inlet valve is connected with the top inlet of condensate liquid collecting tank, the condensate liquid collecting tank
Bottom condensate outlet valve is installed, the outlet of the condensate outlet valve and the raw material of the vacuum material tank upper portion side wall
Tank fluid infusion is connected, and condensate liquid collecting tank steam valve is also associated at the top of the condensate liquid collecting tank, and the condensate liquid is collected
The entrance of tank steam valve is connected with jet chimney.
The reflux drop of top oil removing foam device flows into upper wall stream from the outage of top ring-type catch tray and collects ring, then
Mesospore stream is flowed downwardly into from diversion pipe and collects ring, and the condensation fluid outlet that ring is then collected from mesospore stream enters condensate liquid receipts
Collector；The outage of the reflux drop of middle part oil removing foam device therefrom portion's ring-type catch tray flows into lower wall stream and collects ring, then from
The condensation fluid outlet that lower wall stream collects ring enters condensate collector tube；Reflux drop flows downward along condensate collector tube,
Enter condensate liquid collecting tank from condensate liquid inlet valve.When condensate liquid collecting tank reaches certain liquid level, condensate liquid inlet valve is closed,
Condensate liquid collecting tank steam valve and condensate outlet valve are opened simultaneously, under steam pressure and the suction function of pumped vacuum systems,
Condensate liquid, which enters from head tank fluid infusion in vacuum material tank, is able to reuse, and vacuum depickling system can be mixed into avoid air
In system.
As the further preferred embodiment of the present invention, the fraction between the secondary distillation tower and the condensation recovering device steams
Vapour connecting pipe is more and more lower along airflow direction.Part end vapors touch colder duct wall and are directly condensed into liquid,
It is outwards flowed along connecting pipe, into condensation recovering device, avoids flowing back to destilling tower.
As the present invention preferred embodiment, the condensation recovering device be shell-and-tube heat exchanger, the condensation recovering device it is upper,
Lower both ends are equipped with upper and lower tube sheet, and more cooling water row tubes are connected between upper perforated plate and lower perforated plate；Upper and lower tube sheet is externally connected with
Upper and lower end socket, the inner cavity of upper and lower end socket are divided into left and right hydroecium by end socket partition plate respectively, and the low head is equipped with recover
Cooling water inlet, the upper cover are equipped with recover cooling water outlet；Central partition plate will be in the cylinder of the condensation recovering device
Chamber is divided into left and right gas chamber and the top of left and right gas chamber communicates；The high boiling fraction steam inlet is connected to the left gas chamber
Lower part, the bottom of the left gas chamber are exported equipped with high boiling fraction, the high boiling fraction outlet and high boiling fraction storage tank
Entrance is connected；The low boiler cut steam inlet is connected to the lower part of the right gas chamber, and the upper end of the right gas chamber is equipped with institute
Recover venthole is stated, the bottom of the right gas chamber is exported equipped with low boiler cut, the low boiler cut outlet and low boiling point
The entrance of fraction storage tank is connected.Cooling water enters the left and right hydroecium of low head from recover cooling water inlet respectively, along respective
Cooling water row tube flows up, and enters back into the left and right hydroecium of upper cover, is finally flowed out respectively from recover cooling water outlet.According to
The difference of variety classes fraction boiling point, by adjusting the cooler-water temperature of left and right hydroecium, by low boiler cut and high boiling fraction
It condenses respectively.The low boiler cut steam flowed out from the overhead fraction steam (vapor) outlet of secondary distillation tower is steamed from low boiler cut
Vapour entrance enters the right gas chamber of condensation recovering device, and in flow process from bottom to top, indirect heat exchange, low boiling point are carried out with cooling water
End vapors are condensed into liquid, export and discharge from low boiler cut, into low boiler cut storage tank.From secondary distillation tower
The high boiling fraction steam of portion's end vapors outlet outflow enters the left gas chamber of condensation recovering device from high boiling fraction steam inlet,
In flow process from bottom to top, indirect heat exchange is carried out with cooling water, high boiling fraction steam is condensed into liquid, from higher boiling
Fraction outlets are discharged, into high boiling fraction storage tank.The remaining fraction fat acid vapor not being condensed, from returning for right gas chamber upper end
The discharge of device venthole is received, continues to trap into aliphatic acid trap.
As the further preferred embodiment of the present invention, the trap of the recover venthole and aliphatic acid trap side wall
Air inlet is connected, and the inner cavity top of the aliphatic acid trap is equipped with trap Despumation device, the trap Despumation device
Lower section is equipped with trap spray tube, and the lower section of the trap spray tube is equipped with trap packing layer, the trap air inlet
Positioned at the lower section of the trap packing layer, the top of the aliphatic acid trap is equipped with trap bleeding point, the trap
Bleeding point is connected with pumped vacuum systems, and the bottom of the aliphatic acid trap is exported equipped with trap aliphatic acid, the trap
Aliphatic acid is exported to be connected with the entrance of aliphatic acid pump, and the outlet of the aliphatic acid pump is arranged respectively with fatty acid cycle valve and aliphatic acid
The entrance for putting valve is connected, and the outlet of the fatty acid cycle valve is connected with fatty acid cycle pipe, and the fatty acid cycle pipe goes out
Mouth is connected with the entrance of the trap spray tube；The outlet of the aliphatic acid drain valve is connected with the entrance of fatty acid storage tank.
The fatty acid vapor of the recover that is not condensed condensation enters from trap air inlet in aliphatic acid trap, passes through catch from bottom to top
Storage packing layer, with spray and under low temperature fatty acid liquid carry out sufficient vapour-liquid and contact, directly condense remaining aliphatic acid
Steam, the trap packing layer of ordered structure provide great vapour-liquid contact area, and fatty acid vapor obtains completely herein
Trapping, the water vapour and air not being condensed are evacuated after the drop of Despumation device removal entrainment from trap bleeding point
System is extracted out.The fatty acid liquid of aliphatic acid trap bottom is fallen into, is pumped out by aliphatic acid after heat exchange cools down, through aliphatic acid
Circulating valve and fatty acid cycle pipe enter trap spray tube, carry out circulated sprinkling.When the aliphatic acid of trapping is more and more, fat
When the aliphatic acid liquid level of sour trap bottom is increased to a setting high position, aliphatic acid drain valve is opened, aliphatic acid is sent into aliphatic acid
Storage tank.
As the further preferred embodiment of the present invention, the outlet of the aliphatic acid pump and the aliphatic acid of aliphatic acid heat exchanger change
Hot device aliphatic acid entrance is connected, the outlet of aliphatic acid heat exchanger aliphatic acid and the fatty acid cycle valve of the aliphatic acid heat exchanger
Entrance be connected；The aliphatic acid heat exchanger cooling water inlet of the aliphatic acid heat exchanger is connected with cooling water inlet pipe, the fat
The aliphatic acid heat exchanger cooling water outlet of fat acid heat exchanger is connected with cooling water outlet pipe.The fatty acid solution that aliphatic acid pumps out
Body first enters the cold side of aliphatic acid heat exchanger from aliphatic acid heat exchanger aliphatic acid entrance, is changed with the cooling water of heat absorbing side
It after heat, exports and flows out from aliphatic acid heat exchanger aliphatic acid, then enter fatty acid cycle pipe from fatty acid cycle valve, aliphatic acid is cold
But after, it is more conducive to the fatty acid vapor of trapping.
Description of the drawings
The present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments, attached drawing only provide with reference to
Illustrate to use, it is non-limiting the present invention.
Fig. 1 is the flow chart of the depickling and fraction recovery method of high valent acid vegetable oil of the present invention.
Fig. 2 is the structure diagram of secondary distillation tower in Fig. 1.
Fig. 3 is the enlarged drawing at A positions in Fig. 2.
Fig. 4 is the structure diagram of condensation recovering device in Fig. 1.
Fig. 5 is the structure diagram of aliphatic acid trap in Fig. 1.
Fig. 6 is the stereogram that middle part heater in Fig. 2 is electric heating tube.
Fig. 7 is the stereogram that middle part heater in Fig. 2 is hotline heater.
Fig. 8 is the stereogram that middle part heater in Fig. 2 is steam heater.
In figure：1. secondary distillation tower；1a. destilling tower oil inlet pipes；1b. overhead fraction steam (vapor) outlets；End vapors in the middle part of 1c.
Outlet；1d. destilling tower oil outlets；1e, 1f. condense fluid outlet；Stir steam pipe in 1g. bottoms；2. top oil removing foam device；
2a. rolls over waveform liquid barrier more；2b. drops collect item；2c. ring-type catch trays；3. top heating tank；3a. upper portion heaters；3b.
Top overflow pipe；Stir steam pipe in 3c. tops；4. top oil dispenser；Packing layer on 5.；6. oil-collecting annular groove；7. keep off liquid cover；8.
Oil-collecting annular groove flowline；9. middle part heating tank；Heater in the middle part of 9a.；Overflow pipe in the middle part of 9b.；Stirring steam pipe in the middle part of 9c.；10.
Middle part oil pooling dipper；11. middle part oil dispenser；12. lower packing layer；13. middle part oil removing foam device；14a. upper walls stream collects ring；
14a1. diversion pipes；14b. mesospores stream collects ring；14c. lower walls stream collects ring；15. depickling oil tank；16. vacuum material
Tank；16a. head tank spray tubes；16b. head tank oil outlets；16c. head tank vacuum orifices；16d. head tank fluid infusions；17.
Condensate liquid collecting tank；17a. condensate liquid inlet valves；17b. condensate outlet valves；17c. condensate liquid collecting tank steam valves；18. condensation
Recover；18a. cools down water row tube；18b. low boiler cuts steam inlet；18c. high boiling fractions steam inlet；18d. is recycled
Device venthole；18e. recover cooling water inlets；18f. recover cooling water outlets；18g. end socket partition plates；18h. central partition plates；
18j. low boiler cuts export；18k. high boiling fractions export；19. low boiler cut storage tank；20. high boiling fraction storage tank；21.
Aliphatic acid trap；21a. trap air inlets；21b. trap spray tubes；21c. trap packing layers；21d. traps are taken out
Gas port；21e. traps aliphatic acid exports；21g. trap Despumation devices；21h. trap liquid level gauges；22. fatty acid storage tank；
23. aliphatic acid heat exchanger；23a. aliphatic acid heat exchanger aliphatic acid entrances；23b. aliphatic acid heat exchangers aliphatic acid exports；24. fat
Sour circulating valve；25. aliphatic acid drain valve；26. plant oil heat exchanger.G1. raw material oil pipe；G2. jet chimney；G3. condensate liquid is received
Collector；G4. fatty acid cycle pipe；G5. cooling water inlet pipe；G6. cooling water outlet pipe；B1. crude oil pump；B2. depickling oil pump；
B3. aliphatic acid pumps.
Specific embodiment
As shown in Figure 1, the depickling of high valent acid vegetable oil of the present invention and fraction recovery method in turn include the following steps：100
± 5 DEG C of feedstock oil, which enters in vacuum material tank 16, to be sprayed, and is removed the moisture and air dissolved in feedstock oil, is avoided above-mentioned
Ingredient has a negative impact to oil product in high temperature depickling, and the absolute pressure in vacuum material tank 16 is 2mbar, then raw material
Oil and 225 ± 5 DEG C of high temperature depickling oil carry out indirect heat exchange, and feedstock oil enters back into secondary distillation tower 1 after being warming up to 190 ± 5 DEG C
In carry out first order heating distillation and second level heating distillation successively, oil temperature rises to 220 ± 5 DEG C after the first order heats, through the
Oil temperature rises to 240 ± 5 DEG C after two level heating, oily as described 225 ± 5 DEG C of high temperature depickling after two-step heating distillation, the height
Warm depickling is oily to be reduced to 135 ± 5 DEG C into depickling oil tank with temperature after the feedstock oil indirect heat exchange.
115 ± 5 DEG C of the low boiler cut steam that first order heating distillation generates enters from low boiler cut steam inlet
Condensation recovering device 18 is cooled water indirect condensing into after liquid, into low boiler cut storage tank 19, cooling water inlet temperature 50
DEG C, cooling water outlet temperature is 55 DEG C.
125 ± 5 DEG C of the high boiling fraction steam that second level heating distillation generates enters from high boiling fraction steam inlet
Condensation recovering device 18 is cooled water indirect condensing into after liquid, into high boiling fraction storage tank 20, cooling water inlet temperature 55
DEG C, cooling water outlet temperature is 60 DEG C.
In secondary distillation tower 1, the steam outlet of first order heating distillation and the steam outlet of second level heating distillation
Absolute pressure be 2mbar.
The remaining aliphatic acid vapor (steam) temperature not being condensed in fraction is 80 DEG C, is gone out from the recover on 18 top of condensation recovering device
Steam ports 18d escapes and enter aliphatic acid trap 21, and in aliphatic acid trap 21,50 DEG C of low temperature fatty acid liquid is to fat
Acid vapor carries out circulated sprinkling trapping, the fatty acid liquid temperature of 21 bottom of aliphatic acid trap is fallen into as 60 DEG C, by aliphatic acid
After pump B3 is pumped out, the top that the aliphatic acid trap 21 is returned to after cooling water cools down indirectly is sprayed, cooling water inlet
Temperature is 32 DEG C, and cooling water outlet temperature is 37 DEG C；The top of the aliphatic acid trap 21 is connected with pumped vacuum systems, fat
Absolute pressure in sour trap 21 is 1.5mbar.
The inner cavity top of vacuum material tank 16 is equipped with head tank spray tube 16a, and the head tank at 16 top of vacuum material tank is taken out
Vacuum port 16c is connected with pumped vacuum systems, and the outlet of raw material oil pipe G1 is connected with the entrance of head tank spray tube 16a, and vacuum is former
The head tank oil outlet 16b of 16 bottom of batch can is connected with the entrance of crude oil pump B1, outlet and the plant oil heat exchanger of crude oil pump B1
26 raw material oil inlet is connected, and the material oil outlet of plant oil heat exchanger 26 enters with the destilling tower oil inlet pipe of secondary distillation tower 1
Mouthful connection, the depickling oil of the destilling tower oil outlet 1d of 1 bottom of secondary distillation tower through depickling oil pump B2 and plant oil heat exchanger 26 into
Mouth connection, the depickling oil export of plant oil heat exchanger 26 are connected with depickling oil tank 15.
The overhead fraction steam (vapor) outlet 1b of the secondary distillation tower 1 and low boiler cut steam inlet 18b of condensation recovering device 18
Connection, the middle part end vapors outlet 1c and the high boiling fraction steam inlet 18c of condensation recovering device 18 of secondary distillation tower 1 connect
It connects.End vapors connecting pipe between secondary distillation tower 1 and condensation recovering device 18 is more and more lower along airflow direction.Part fraction
Steam touches colder duct wall and is directly condensed into liquid, outwards flows along connecting pipe, into condensation recovering device 18, keeps away
Exempt to flow back to destilling tower 1.
Pumped vacuum systems carries out suction by head tank vacuum orifice 16c makes the inner cavity of vacuum material tank 16 be in vacuum shape
State, the high valent acid vegetable oil that preceding working procedure is come enter head tank spray tube 16a through raw material oil pipe G1 and are sprayed.It is taken off by vacuum
Vegetable oil after gas is flowed out from the head tank oil outlet 16b of 16 bottom of vacuum material tank, and vegetable oil heat exchange is sent by crude oil pump B1
The depickling oil of device 26 and high temperature carries out indirect heat exchange, and the oil temperature of depickling oil declines, and the oil temperature of feedstock oil raises, then feedstock oil from
The material oil outlet outflow of plant oil heat exchanger 26, into the destilling tower oil inlet pipe 1a of secondary distillation tower 1, in secondary distillation tower 1
It is middle that first the low boiler cut in vegetable oil is evaporated through low temperature distillation, then evaporate the higher boiling in vegetable oil through high temperature distillation
Divide and be evaporated；Low boiler cut steam is discharged from the overhead fraction steam (vapor) outlet 1b of secondary distillation tower 1, is steamed from low boiler cut
Vapour entrance 18b enters condensation recovering device 18 and condenses；High boiling fraction steam exports 1c from the middle part end vapors of secondary distillation tower 1
Discharge, from high boiling fraction steam inlet, 18c enters condensation recovering device 18 and condenses, low boiler cut and higher boiling in vegetable oil
Fraction is able to be separated from vegetable oil respectively.
Depickling oil after two level depickling is flowed out from the destilling tower oil outlet 1d of 1 bottom of secondary distillation tower, by depickling oil pump
B2 is pumped into the depickling oil inlet of plant oil heat exchanger 26, and after being preheated to feedstock oil, depickling oil is from plant oil heat exchanger 26
Depickling oil export flows out, into depickling oil tank 15.
As shown in Fig. 2, overhead fraction steam (vapor) outlet 1b is located at the top center of secondary distillation tower 1, overhead fraction steam goes out
Mouth 1b's is arranged right below top oil removing foam device 2, and the lower section of top oil removing foam device 2 is equipped with top heating tank 3, top heating
Slot 3 is fixed on the inner wall circumference of secondary distillation tower 1 and open top, the outlet insertion top heating tank of destilling tower oil inlet pipe 1a
Below 3 pasta, it is equipped with upper portion heater 3a in top heating tank 3 and top overflow pipe 3b, the bottom of top heating tank 3 is equipped with
Top stirs steam pipe 3c, the lower end of top overflow pipe 3b through top heating tank 3 bottom wall and enter with top oil dispenser 4
Mouth is connected, and the lower section of top oil dispenser 4 is equipped with upper packing layer 5；The lower section of upper packing layer 5 is equipped with and is fixed on secondary distillation tower 1
Oil-collecting annular groove 6 on inner wall, the centre bore top of oil-collecting annular groove 6 are equipped with gear liquid cover 7；The bottom of oil-collecting annular groove 6 is connected with oil-collecting
Annular groove flowline 8, the lower end of oil-collecting annular groove flowline 8 are inserted into below the pasta of middle part heating tank 9, are equipped in middle part heating tank 9
Middle part heater 9a and middle part overflow pipe 9b, the bottom of middle part heating tank 9 are equipped with middle part and stir steam pipe 9c, middle part overflow pipe 9b
Lower end through middle part heating tank 9 bottom wall and insertion middle part oil pooling dipper 10 pasta below, the outlet of middle part oil pooling dipper 10 with
The entrance of middle part oil dispenser 11 is connected, and the lower section of middle part oil dispenser 11 is equipped with lower packing layer 12；Middle part oil pooling dipper 10 is in
Middle part oil removing foam device 13 is equipped between portion's heating tank 9, middle part end vapors outlet 1c is located at middle part oil removing foam device 13 in
Between portion's heating tank 9；The bottom of secondary distillation tower 1 is equipped with bottom stirring steam pipe 1g.
Vegetable oil after vacuum outgas enters from the destilling tower oil inlet pipe 1a of secondary distillation tower 1 in top heating tank 3,
The multiple baffling in top heating tank 3, and it is subject to the strong stirring of the live (open) steam of top stirring steam pipe 3c injections, on top
Under the heating of heater 3a, oil temperature is increased to after setting technological temperature to flow out from top overflow pipe 3b to underflow stream, through top oil
Uniformly spread in upper packing layer 5, carries out in upper packing layer 5 with the stirring steam in middle part heating tank 9 after the distribution of distributor 4
Full regression gas-liquid contact, the low boiler cut in vegetable oil constantly evaporates under water vapor acting, in vacuum power source
Suction under, low boiler cut steam flows upward, after 2 foam removal of top oil removing foam device, from the top of secondary distillation tower 1
The overhead fraction steam (vapor) outlet 1b outflows of the heart；
The vegetable oil of removing low boiler cut is fallen into after spilling from upper packing layer 5 in oil-collecting annular groove 6, then is gone out from oil-collecting annular groove
Oil pipe 8 is flowed into the heating tank 9 of middle part, the multiple baffling in middle part heating tank 9, and is subject to the straight of middle part stirring steam pipe 9c injections
The strong stirring of steam is connect, under the heating of middle part heater 9a, oil temperature continues after raising from middle part overflow pipe 9b to underflow stream
Into middle part oil pooling dipper 10；Middle part oil pooling dipper 10 plays the role of fluid-tight, plant between the top of secondary distillation tower 1 and middle part
Oil is after the outflow of middle part oil pooling dipper 10, and uniformly spread is in lower packing layer 12 after the distribution of middle part oil dispenser 11, in lower filler
Carry out full regression gas-liquid contact in layer 12 with the stirring steam of bottom stirring steam pipe 1g injection, the higher boiling in vegetable oil evaporates
Divide and constantly evaporated under water vapor acting, under the suction of vacuum power source, high boiling fraction steam flows upward passes through
After 13 foam removal of middle part oil removing foam device, from the middle part end vapors outlet 1c outflows of secondary distillation tower 1.
Vegetable oil after secondary distillation falls into the bottom of secondary distillation tower 1, is flowed out from destilling tower oil outlet 1d.
As shown in Figures 2 and 3, on the ventilation section of 13 central upper portion of top oil removing foam device 2 and middle part oil removing foam device
More folding waveform liquid barrier 2a are respectively equipped with, the lower end peripheries for rolling over waveform liquid barrier 2a are connected to annular catch tray 2c, ring more
The excircle of shape catch tray 2c is tilted down and is connected on the inner wall of secondary distillation tower 1；Under each more folding waveform liquid barrier 2a
Edge is respectively equipped with the drop collection 2b that drop is oriented to annular catch tray 2c, and the lowest part of annular catch tray 2c is respectively equipped with row
Fluid apertures.
When low boiler cut steam flows through more folding waveform liquid barrier 2a of top oil removing foam device 2, high boiling fraction steam
When flowing through more folding waveform liquid barriers of middle part oil removing foam device 13, drop is blocked respectively, and collecting a 2b by drop flows into ring
Shape catch tray 2c, then flowed downward out from the outage of annular catch tray 2c lowest parts along the barrel of secondary distillation tower 1.
Upper wall stream is equipped with below the annular catch tray 2c of top oil removing foam device 2 and collects ring 14a, top heating tank 3 with
Mesospore stream is equipped between top oil dispenser 4 and collects ring 14b, the lowest part that upper wall stream collects ring 14a is connected with diversion pipe
The lower end aligned mesospore stream of 14a1, diversion pipe 14a1 collect ring 14b；It is set below the annular catch tray of middle part oil removing foam device 13
There is lower wall stream to collect ring 14c, the lowest part that mesospore stream collects ring 14b is equipped with condensation fluid outlet 1e, and lower wall stream collects ring
The lowest part for enclosing 14c is equipped with condensation fluid outlet 1f, condenses fluid outlet 1e and is stretched respectively with the external end head for condensing fluid outlet 1f
Go out outside the cylinder of secondary distillation tower 1 and be connected respectively with condensate collector tube G3, the outlet of condensate collector tube G3 and condensate liquid
The entrance of inlet valve 17a is connected, and the outlet of condensate liquid inlet valve 17a is connected with the top inlet of condensate liquid collecting tank 17, cold
The bottom of lime set collecting tank 17 is equipped with condensate outlet valve 17b, the outlet of condensate outlet valve 17b on vacuum material tank 16
The head tank fluid infusion 16d of portion's side wall is connected, and the top of condensate liquid collecting tank 17 is also associated with condensate liquid collecting tank steam valve
17c, the entrance of condensate liquid collecting tank steam valve 17c are connected with jet chimney G2.
The reflux drop of top oil removing foam device 2 flows into upper wall stream from the outage of top ring-type catch tray and collects ring
14a, then flow downwardly into mesospore stream from diversion pipe 14a1 and collect ring 14b, the condensation liquid stream of ring 14b is then collected from mesospore stream
Outlet 1e enters condensate collector tube G3；The outage stream of the reflux drop of middle part oil removing foam device 13 therefrom portion's ring-type catch tray
Enter lower wall stream and collect ring 14c, then enter condensate collector tube G3 from the condensation fluid outlet 1f of lower wall stream collection ring 14c；
Reflux drop flows downward along condensate collector tube G3, enters condensate liquid collecting tank 17 from condensate liquid inlet valve 17a.Work as condensate liquid
When collecting tank 17 reaches certain liquid level, condensate liquid inlet valve 17a is closed, opens simultaneously condensate liquid collecting tank steam valve 17c and cold
Condensate outlet valve 17b, under steam pressure and the suction function of pumped vacuum systems, condensate liquid i.e. from head tank fluid infusion 16d into
Enter and reuse is able in vacuum material tank 16, and can be mixed into avoid air in vacuum deacidification system.
As shown in Figure 6 to 8, middle part heater 9a can be electric heater, hotline heater and steam heater, on
Portion heater 3a is also such.According to different oil product and technological requirement, different heaters can be selected.
As shown in figure 4, condensation recovering device 18 is shell-and-tube heat exchanger, the upper/lower terminal of condensation recovering device 18 is equipped with above and below
Tube sheet is connected with more cooling water row tube 18a between upper perforated plate and lower perforated plate；Upper and lower tube sheet is externally connected with upper and lower end socket, upper,
The inner cavity of low head is divided into left and right hydroecium by end socket partition plate 18g respectively, and low head is equipped with recover cooling water inlet 18e,
Upper cover is equipped with recover cooling water outlet 18f；The cylinder lumen of condensation recovering device 18 is divided into left and right by central partition plate 18h
The top of gas chamber and left and right gas chamber communicates；High boiling fraction steam inlet 18c is connected to the lower part of left gas chamber, the bottom of left gas chamber
18k is exported equipped with high boiling fraction, high boiling fraction outlet 18k is connected with the entrance of high boiling fraction storage tank 20；Low boiling point evaporates
Point steam inlet 18b is connected to the lower part of right gas chamber, and the upper end of right gas chamber is equipped with recover venthole 18d, the bottom of right gas chamber
18j is exported equipped with low boiler cut, low boiler cut outlet 18j is connected with the entrance of low boiler cut storage tank 19.
Cooling water enters the left and right hydroecium of low head from recover cooling water inlet 18e respectively, is arranged along respective cooling water
Pipe 18a is flowed up, and enters back into the left and right hydroecium of upper cover, is finally flowed out respectively from recover cooling water outlet 18f.According to not
With the difference of species fraction boiling point, by adjusting the cooler-water temperature of left and right hydroecium, by low boiler cut and high boiling fraction point
It does not condense.
From the low boiler cut steam that the overhead fraction steam (vapor) outlet 1b of secondary distillation tower 1 flows out from low boiler cut steam
Entrance 18b enters the right gas chamber of condensation recovering device 18, and in flow process from bottom to top, indirect heat exchange is carried out with cooling water, low
Boiling point fraction steam is condensed into liquid, from low boiler cut outlet 18j discharges, into low boiler cut storage tank 19.
From the high boiling fraction steam of the middle part end vapors outlet 1c outflows of secondary distillation tower 1 from high boiling fraction steam
Entrance 18c enters the left gas chamber of condensation recovering device 18, and in flow process from bottom to top, indirect heat exchange is carried out with cooling water, high
Boiling point fraction steam is condensed into liquid, from high boiling fraction outlet 18k discharges, into high boiling fraction storage tank 20.
The remaining end vapors not being condensed, predominantly fatty acid vapor, the recover venthole 18d from right gas chamber upper end
Discharge, continues to trap into aliphatic acid trap 21.
As shown in figure 5, recover venthole 18d is connected with the trap air inlet 21a of 21 side wall of aliphatic acid trap, fat
The inner cavity top of fat acid trap 21 is equipped with trap Despumation device 21g, and the lower section of trap Despumation device 21g is equipped with trap
The lower section of spray tube 21b, trap spray tube 21b are equipped with trap packing layer 21c, and trap air inlet 21a is located at trap
The lower section of packing layer 21c, the top of aliphatic acid trap 21 are equipped with trap bleeding point 21d, trap bleeding point 21d with taking out very
Empty set system is connected, and the bottom of aliphatic acid trap 21 is equipped with trap aliphatic acid and exports 21e, trap aliphatic acid outlet 21e with
The entrance of aliphatic acid pump B3 is connected, and the outlet of aliphatic acid pump B3 enters respectively with fatty acid cycle valve 24 and aliphatic acid drain valve 25
Mouth is connected, and the outlet of fatty acid cycle valve 24 is connected with fatty acid cycle pipe G4, the outlet of fatty acid cycle pipe G4 and trap
The entrance of spray tube 21b is connected；The outlet of aliphatic acid drain valve 25 is connected with the entrance of fatty acid storage tank 22.Aliphatic acid trap
21 lower part is equipped with trap liquid level gauge 21h.
The fatty acid vapor of the recover 18 that is not condensed condensation enters aliphatic acid trap 21 from trap air inlet 21a
In, from bottom to top through trap packing layer 21c, with spray and under low temperature fatty acid liquid carry out sufficient vapour-liquid and contact,
Remaining fatty acid vapor is directly condensed, the trap packing layer 21c of ordered structure provides great vapour-liquid contact area, fat
Fat acid vapor is trapped completely herein, after the drop that the water vapour and air not being condensed are carried secretly through Despumation device removal,
System extraction is evacuated from trap bleeding point 21d.The fatty acid liquid of 21 bottom of aliphatic acid trap is fallen into, by aliphatic acid
Pump B3 is pumped out, and is entered trap spray tube 21b through fatty acid cycle valve 24 and fatty acid cycle pipe G4, is carried out circulated sprinkling.When
The aliphatic acid of trapping is more and more, and when trap liquid level gauge 21h detects a setting high position, control system opens aliphatic acid drain valve
25, aliphatic acid is sent into fatty acid storage tank 22.
As shown in Figure 1, the outlet of aliphatic acid pump B3 and the aliphatic acid heat exchanger aliphatic acid entrance 23a of aliphatic acid heat exchanger 23
It is connected, the aliphatic acid heat exchanger aliphatic acid outlet 23b of aliphatic acid heat exchanger 23 is connected with the entrance of fatty acid cycle valve 24；Fat
The aliphatic acid heat exchanger cooling water inlet of sour heat exchanger 23 is connected with cooling water inlet pipe G5, the aliphatic acid of aliphatic acid heat exchanger 23
Heat exchanger cooling water outlet is connected with cooling water outlet pipe G6.
The fatty acid liquid that aliphatic acid pump B3 is pumped out, first enters aliphatic acid from aliphatic acid heat exchanger aliphatic acid entrance 23a and changes
The cold side of hot device, after being exchanged heat with the cooling water of heat absorbing side, from aliphatic acid heat exchanger aliphatic acid outlet 23b outflows, then from
Fatty acid cycle valve 24 enters fatty acid cycle pipe G4, after aliphatic acid is cooled, is more conducive to the fatty acid vapor of trapping, simultaneously
The heat in aliphatic acid can be recycled.
The foregoing is merely the preferable possible embodiments of the present invention, non-therefore the limitation present invention patent protection model
It encloses.In addition to the implementation, the present invention can also have other embodiment.All skills formed using equivalent substitution or equivalent transformation
Art scheme, all fall within the present invention claims protection domain in.Technical characteristic of the present invention without description can be by or using now
There is technology realization, details are not described herein.
Claims (9)
1. a kind of depickling of high valent acid vegetable oil and fraction recovery method, which is characterized in that in turn include the following steps：Feedstock oil
It is sprayed into vacuum material tank, removes the moisture and air dissolved in feedstock oil, then feedstock oil and high temperature depickling oil
Indirect heat exchange is carried out, is entered back into after feedstock oil heating in secondary distillation tower and carries out first order heating distillation and second level heating successively
Distillation, becomes high temperature depickling oil after two-step heating distillation, the high temperature depickling is oily laggard with the feedstock oil indirect heat exchange
Enter depickling oil tank；The low boiler cut steam that first order heating distillation generates enters from low boiler cut steam inlet to be condensed back to
It receives device and is cooled water indirect condensing into after liquid, into low boiler cut storage tank；The higher boiling that second level heating distillation generates evaporates
Point steam enters condensation recovering device from high boiling fraction steam inlet and is cooled water indirect condensing into after liquid, is evaporated into higher boiling
Divide storage tank；The fatty acid vapor of residue not being condensed in fraction, goes forward side by side from the recover venthole discharge on condensation recovering device top
Enter aliphatic acid trap, in the aliphatic acid trap, low temperature fatty acid liquid carries out circulated sprinkling to fatty acid vapor and catches
Collection, falls into the fatty acid liquid of aliphatic acid trap bottom, after being pumped out by aliphatic acid, institute is returned to after cooling water cools down indirectly
It states and is sprayed at the top of aliphatic acid trap；The top of the aliphatic acid trap is connected with pumped vacuum systems；The recycling
Device venthole is connected with the trap air inlet of aliphatic acid trap side wall, and the inner cavity top of the aliphatic acid trap, which is equipped with, catches
Storage Despumation device, the lower section of the trap Despumation device are equipped with trap spray tube, the lower section of the trap spray tube
Equipped with trap packing layer, the trap air inlet is located at the lower section of the trap packing layer, the aliphatic acid trap
Top be equipped with trap bleeding point, the trap bleeding point is connected with pumped vacuum systems, the bottom of the aliphatic acid trap
Portion is exported equipped with trap aliphatic acid, and the trap aliphatic acid outlet is connected with the entrance of aliphatic acid pump, the aliphatic acid pump
Entrance of the outlet respectively with fatty acid cycle valve and aliphatic acid drain valve be connected, outlet and the fat of the fatty acid cycle valve
Sour circulation pipe is connected, and the outlet of the fatty acid cycle pipe is connected with the entrance of the trap spray tube；The aliphatic acid row
The outlet for putting valve is connected with the entrance of fatty acid storage tank.
2. the depickling of high valent acid vegetable oil according to claim 1 and fraction recovery method, it is characterised in that：The raw material
The temperature of oil is 100 ± 5 DEG C, and with being warming up to 190 ± 5 DEG C after high temperature depickling oil heat exchange, oil temperature rises to 220 after the first order heats
± 5 DEG C, oil temperature rises to 240 ± 5 DEG C after the second level is heated, and the temperature before the oily heat exchange with the feedstock oil of the high temperature depickling is
225 ± 5 DEG C, the temperature after heat exchange is 135 ± 5 DEG C；The low boiler cut vapor (steam) temperature of secondary distillation tower discharge for 115 ±
5 DEG C, the high boiling fraction vapor (steam) temperature of the secondary distillation tower discharge is 125 ± 5 DEG C；It is discharged from the condensation recovering device surplus
Remaining aliphatic acid vapor (steam) temperature is 80 DEG C, and in the aliphatic acid trap, the spray temperature of low temperature fatty acid liquid is 50 DEG C；It is described
Absolute pressure in aliphatic acid trap is 1.5mbar, the first order in the vacuum material tank and the secondary distillation tower
The absolute pressure of heating distillation and second level heating distillation is 2mbar.
3. the depickling of high valent acid vegetable oil according to claim 1 or 2 and fraction recovery method, it is characterised in that：It is described
The inner cavity top of vacuum material tank be equipped with head tank spray tube, the head tank vacuum orifice of the vacuum material tank top with it is described
Pumped vacuum systems connects, and the outlet of raw material oil pipe is connected with the entrance of the head tank spray tube, the vacuum material pot bottom
Head tank oil outlet and crude oil pump entrance connect, the crude oil pump outlet and plant oil heat exchanger raw material oil inlet phase
Even, the material oil outlet of the plant oil heat exchanger is connected with the entrance of the destilling tower oil inlet pipe of secondary distillation tower, the two level
The destilling tower oil outlet of distillation tower bottom is connected through depickling oil pump with the depickling oil inlet of plant oil heat exchanger, and the vegetable oil changes
The depickling oil export of hot device is connected with depickling oil tank；The overhead fraction steam (vapor) outlet of the secondary distillation tower and the condensation
The low boiler cut steam inlet connection of recover, middle part end vapors outlet and the condensation of the secondary distillation tower are recycled
The high boiling fraction steam inlet connection of device, the recover venthole of the condensation recovering device are connected with the pumped vacuum systems.
4. the depickling of high valent acid vegetable oil according to claim 3 and fraction recovery method, it is characterised in that：The top
End vapors outlet is located at the top center of the secondary distillation tower, and the overhead fraction steam (vapor) outlet is arranged right below top
Oil removing foam device, the lower section of the top oil removing foam device are equipped with top heating tank, and the top heating tank is fixed on described two
The pasta of the top heating tank is inserted on the inner wall circumference of grade destilling tower and open top, the outlet of the destilling tower oil inlet pipe
Hereinafter, upper portion heater and top overflow pipe are equipped in the top heating tank, the bottom of the top heating tank is equipped with top
Stir steam pipe, the lower end of the top overflow pipe through the top heating tank bottom wall and with the entrance of top oil dispenser
It is connected, the lower section of the top oil dispenser is equipped with upper packing layer；The lower section of the upper packing layer is equipped with and is fixed on the two level
The oil-collecting annular groove on inner wall of tower is distilled, gear liquid cover is equipped with above the centre bore of the oil-collecting annular groove；The bottom of the oil-collecting annular groove
Oil-collecting annular groove flowline is connected with, the lower end of the oil-collecting annular groove flowline is inserted into below the pasta of middle part heating tank, in described
Middle part heater and middle part overflow pipe are equipped in portion's heating tank, the bottom of the middle part heating tank is equipped with middle part and stirs steam pipe,
The lower end of the middle part overflow pipe is passed through below the pasta of the bottom wall of the middle part heating tank and insertion middle part oil pooling dipper, in described
The outlet of portion's oil pooling dipper is connected with the entrance of middle part oil dispenser, and the lower section of the middle part oil dispenser is equipped with lower packing layer；Institute
It states and oil removing foam device in middle part is equipped between middle part oil pooling dipper and the middle part heating tank, the middle part end vapors outlet is located at institute
It states between middle part oil removing foam device and the middle part heating tank；The bottom of the secondary distillation tower is equipped with bottom and stirs steam pipe.
5. the depickling of high valent acid vegetable oil according to claim 4 and fraction recovery method, it is characterised in that：The top
More folding waveform liquid barriers are respectively equipped on oil removing foam device and the ventilation section of the middle part oil removing foam device central upper portion, it is described
The lower end peripheries of more folding waveform liquid barriers are connected to annular catch tray, the excircle of the ring-type catch tray tilt down and
It is connected on the inner wall of the secondary distillation tower；Described in the lower edges of each more folding waveform liquid barriers are respectively equipped with and are oriented to drop
The drop of annular catch tray collects item, and the lowest part of the ring-type catch tray is respectively equipped with outage.
6. the depickling of high valent acid vegetable oil according to claim 5 and fraction recovery method, it is characterised in that：The top
Upper wall stream is equipped with below the annular catch tray of oil removing foam device and collects ring, the top heating tank and the top oil dispenser
Between be equipped with mesospore stream and collect ring, the lowest part that the upper wall stream collects ring is connected with diversion pipe, under the diversion pipe
End is directed at the mesospore stream and collects ring；Lower wall stream is equipped with below the annular catch tray of the middle part oil removing foam device and collects ring
Circle, the mesospore stream collects ring and the lowest part of lower wall stream collection ring is respectively equipped with condensation fluid outlet, described cold
The external end head of lime set outflux is stretched out outside the cylinder of the secondary distillation tower and is connected respectively with condensate collector tube respectively, described
The outlet of condensate collector tube is connected with the entrance of condensate liquid inlet valve, and outlet and the condensate liquid of the condensate liquid inlet valve are collected
The top inlet of tank is connected, and the bottom of the condensate liquid collecting tank is equipped with condensate outlet valve, the condensate outlet valve
Outlet be connected with the head tank fluid infusion of the vacuum material tank upper portion side wall, be also connected at the top of the condensate liquid collecting tank
There is condensate liquid collecting tank steam valve, the entrance of the condensate liquid collecting tank steam valve is connected with jet chimney.
7. the depickling of high valent acid vegetable oil according to claim 3 and fraction recovery method, it is characterised in that：The two level
End vapors connecting pipe between destilling tower and the condensation recovering device is more and more lower along airflow direction.
8. the depickling of high valent acid vegetable oil according to claim 1 or 2 and fraction recovery method, it is characterised in that：It is described
Condensation recovering device is shell-and-tube heat exchanger, and the upper/lower terminal of the condensation recovering device is equipped with upper and lower tube sheet, upper perforated plate and down tube
More cooling water row tubes are connected between plate；Upper and lower tube sheet is externally connected with upper and lower end socket, the inner cavity of upper and lower end socket respectively by
End socket partition plate is divided into left and right hydroecium, and the low head is equipped with recover cooling water inlet, and the upper cover is equipped with recycling
Device cooling water outlet；The cylinder lumen of the condensation recovering device is divided into the top of left and right gas chamber and left and right gas chamber by central partition plate
It communicates；The high boiling fraction steam inlet is connected to the lower part of the left gas chamber, and the bottom of the left gas chamber is equipped with higher boiling
Fraction outlets, the high boiling fraction outlet are connected with the entrance of high boiling fraction storage tank；The low boiler cut steam inlet
The lower part of the right gas chamber is connected to, the upper end of the right gas chamber is equipped with the recover venthole, the bottom of the right gas chamber
It is exported equipped with low boiler cut, the low boiler cut outlet is connected with the entrance of low boiler cut storage tank.
9. the depickling of high valent acid vegetable oil according to claim 1 and fraction recovery method, it is characterised in that：The fat
The outlet of acid pump is connected with the aliphatic acid heat exchanger aliphatic acid entrance of aliphatic acid heat exchanger, the aliphatic acid of the aliphatic acid heat exchanger
The outlet of heat exchanger aliphatic acid is connected with the entrance of the fatty acid cycle valve；The aliphatic acid heat exchanger of the aliphatic acid heat exchanger is cold
But water inlet is connected with cooling water inlet pipe, and the aliphatic acid heat exchanger cooling water outlet of the aliphatic acid heat exchanger goes out with cooling water
Water pipe is connected.
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| CN108795566A (en) * | 2018-05-24 | 2018-11-13 | 新疆泰昆集团股份有限公司 | A kind of device removing cyclopropene fatty acid containment trans-fatty acid in two level cotton oil |
| CN112521990A (en) * | 2020-11-16 | 2021-03-19 | 四川金尚环保科技有限公司 | Method for producing high-flash-point pure oil fuel by modifying methanol with waste cooking oil |
| CN113512464A (en) * | 2021-05-10 | 2021-10-19 | 江苏旗云油脂科技有限公司 | Method for preparing grease |
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| CN104508100A (en) * | 2012-07-12 | 2015-04-08 | 阿尔法拉瓦尔股份有限公司 | Deacidification of fats and oils |
| CN202898386U (en) * | 2012-10-19 | 2013-04-24 | 武汉工业学院 | High acid value oil physical distillation deacidification device |
| CN103320220A (en) * | 2013-07-19 | 2013-09-25 | 河南华泰粮油机械工程有限公司 | Method for distilling and refining high-grade oil by rice bran oil molecules |
| CN103805337A (en) * | 2014-01-10 | 2014-05-21 | 陈汉卿 | Rice bran oil refining method |
| CN104194929A (en) * | 2014-09-04 | 2014-12-10 | 陈汉卿 | Grease refining system |
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