CN104928024A - Deacidification and fraction recovery method for high acid value vegetable oil - Google Patents
Deacidification and fraction recovery method for high acid value vegetable oil Download PDFInfo
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- CN104928024A CN104928024A CN201510321598.9A CN201510321598A CN104928024A CN 104928024 A CN104928024 A CN 104928024A CN 201510321598 A CN201510321598 A CN 201510321598A CN 104928024 A CN104928024 A CN 104928024A
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Abstract
The invention relates to a deacidification and fraction recovery method for high acid value vegetable oil. The method sequentially comprises the steps that raw oil carries out indirect heat exchange with high-temperature deacidified oil after vacuum degassing, then first-grade heating and distillation and second-grade heating and distillation are carried out in sequence, and high-temperature deacidified oil is obtained after two grades of heating and distillation; low boiling point fraction steam produced through first-stage heating and distillation enters a condensation recycler to be condensed in a liquid state, and then enters a low boiling point fraction storage pot; high boiling point fraction steam produced through second-stage heating and distillation enters a condensation recycler to be condensed in a liquid state, and then enters a high boiling point fraction storage pot; residual fatty acid steam not condensed in the fraction enters a fatty acid collector to be sprayed and collected by low-temperature fatty acid liquid; the top of the fatty acid collector is connected with a vacuum-pumping system. According to the deacidification and fraction recovery method for high acid value vegetable oil, the requirement for the finished product acid value of the high acid value vegetable oil is met, neutral oil losses produced in the deacidification process are small, graded recycle can be achieved for low boiling point fraction and high boiling point fraction, and follow-up purification investment is reduced.
Description
Technical field
The present invention relates to a kind of depickling and cut recovery method of high valent acid vegetable oil, belong to vegetables oil processing technique field.
Background technology
Depickling is very important link in vegetable oil fine sweetening process, and deacidifying device quality determines the success or failure of deacidifying process.The method of the physical deacidification of the high valent acid vegetable oil adopting high temperature high vacuum to be undertaken by steam distillation principle; without the need to the chemical deacidification by adding alkali, not producing waste water, being conducive to protection of the environment; greatly improve product (oil) yield, and the acid byproduct fatty of high added value can be obtained.
In recent years, ordered structure filler is simple with its structure, steam utilization efficiency is high, the advantages such as the vapour-liquid ratio area provided is large are promoted rapidly, current most of production line uses filler extracting tower, for the grease of high acid value, need overhead oil ingress obtain very high oil temperature provide all lipid acid evaporate needed for heat, too high oil temperature can cause the polymerization of grease, decomposition, trans fatty acid to increase, if turn down oil inlet temperature, packing tower middle and lower part declines because oil temperature reduces deacidification effect, and depickling is not thorough.Secondly the oil product of high acid value is in the easy flash distillation of tower top high oil temperature, and significant quantities of fat acid vapour can cause the carrying secretly of neutral oil, product loss, distills out acid byproduct fatty purity not high; The depickling of the more general oil product of the bed stuffing height needed for oil product depickling of high acid value in addition, deodorization want high, the pressure drop that too high packing layer brings, and vacuum tightness at the bottom of bottom column is declined, and depickling ability reduces, and at the bottom of tower, depickling oleic acid value is difficult to meet processing requirement.
Reclaim for distilling out lipid acid, generally adopt the fatty acid liquid spray of single-stage filler trap low temperature to trap at present and distill out lipid acid steam, what obtain is mixed fatty acid, increases the investment of the separating-purifying of follow-up acid byproduct fatty.
Summary of the invention
The object of the invention is to, overcome problems of the prior art, there is provided a kind of depickling and cut recovery method of high valent acid vegetable oil, deacidification effect meets processing requirement, carries out classification recovery to the low boiler cut in high valent acid vegetable oil and high boiling fraction simultaneously.
For solving above technical problem, the depickling of a kind of high valent acid vegetable oil of the present invention and cut recovery method, in turn include the following steps: stock oil enters in vacuum material tank and sprays, remove the moisture and air that dissolve in stock oil, then stock oil and high temperature depickling oil carry out indirect heat exchange, stock oil enters in secondary distillation tower after heating up again and carries out the first step successively and add thermal distillation and the second stage adds thermal distillation, become described high temperature depickling oil after two-step heating distillation, after described high temperature depickling oil and described stock oil indirect heat exchange, enter depickling oil tank; The first step adds low boiler cut steam that thermal distillation produces and enters condensation recovering device from low boiler cut steam-in and be cooled after water indirect condensing becomes liquid state, enters low boiler cut storage tank; The second stage adds high boiling fraction steam that thermal distillation produces and enters condensation recovering device from high boiling fraction steam-in and be cooled after water indirect condensing becomes liquid state, enters high boiling fraction storage tank; The residue lipid acid steam be not condensed in cut, lipid acid trap is escaped and enter from the withdrawer steam outlet on condensation recovering device top, in described lipid acid trap, low temperature fatty acid liquid carries out circulated sprinkling trapping to lipid acid steam, fall into the fatty acid liquid of lipid acid trap bottom, after being pumped by lipid acid pump, the top getting back to described lipid acid trap after water coolant is lowered the temperature indirectly sprays; The top of described lipid acid trap is connected with pumped vacuum systems.
Relative to prior art, the present invention achieves following beneficial effect: pumped vacuum systems is undertaken aspirating by head tank vacuum orifice makes the inner chamber of vacuum material tank be in vacuum state, the high valent acid vegetable oil that former process is come sprays through the incoming stock tank shower of raw material oil pipe, due to distributing of nozzle, the moisture dissolved in vegetables oil, oxygen, air are removed clean, avoids mentioned component to have a negative impact to oil product when high temperature depickling; Vegetables oil after vacuum outgas flows out from the head tank oil outlet of vacuum material pot bottom, the depickling oil being sent into vegetables oil interchanger and high temperature by crude oil pump carries out indirect heat exchange, the oil temperature of depickling oil declines, the oil temperature of stock oil raises, then stock oil flows out from the material oil outlet of vegetables oil interchanger, enter the distillation tower oil inlet pipe of secondary distillation tower, in secondary distillation tower, vegetables oil is by gradient-heated at twice, but obtains condition of high vacuum degree unanimous between the higher and lower levels.The temperature of first step heating is slightly low, slightly low distillation temperature realizes low boiler cut such as low carbon chain lipid acid and to volatilize from oil spilling, the components such as lipid acid are utilized to have boiling point difference, in oil, low boiler cut preferentially removes, discharge from the overhead fraction vapour outlet of secondary distillation tower, enter condensation recovering device condensation from low boiler cut steam-in.Oil after one-level distillation reaches higher distillation temperature after secondary heating, ensure the acid number requirement of depickling oil, high boiling fraction such as high carbon chain fatty acid distillation goes out by secondary distillation, high boiling fraction is discharged from the middle part end vapors outlet of secondary distillation tower, enters condensation recovering device condensation from high boiling fraction steam-in.Shorten vegetables oil while fractional distillation and recovery enhance deacidification effect through the pyrogenous time, be conducive to the nutritive ingredients such as VE in oil, plant sterol, thiaminogen and retain.Depickling oil after secondary depickling flows out from the distillation tower oil outlet of secondary distillation tower bottom, the depickling oil inlet of vegetables oil interchanger is pumped into by depickling oil pump, after carrying out preheating to stock oil, depickling oil flows out from the depickling oil export of vegetables oil interchanger, enters depickling oil tank.Both reclaimed the heat of depickling oil, reduced the temperature of depickling oil, and made again stock oil obtain preheating, reduce energy consumption.
As preferred version of the present invention, the temperature of described stock oil is 100 ± 5 DEG C, 190 ± 5 DEG C are warming up to after the heat exchange of high temperature depickling oil, after first step heating, oil temperature rises to 220 ± 5 DEG C, after the heating of the second stage, oil temperature rises to 240 ± 5 DEG C, temperature before described high temperature depickling oil and described stock oil heat exchange is 225 ± 5 DEG C, and the temperature after heat exchange is 135 ± 5 DEG C; The low boiler cut vapor temperature of described secondary distillation tower discharge is 115 ± 5 DEG C, and the high boiling fraction vapor temperature of described secondary distillation tower discharge is 125 ± 5 DEG C; The residue lipid acid vapor temperature of discharging from described condensation recovering device is 80 DEG C, and in described lipid acid trap, the spray temperature of low temperature fatty acid liquid is 50 DEG C; Absolute pressure in described lipid acid trap is 1.5mbar, and the first step in described vacuum material tank and described secondary distillation tower adds the absolute pressure that thermal distillation and the second stage adds thermal distillation and is 2mbar.
As preferred version of the present invention, the inner chamber top of described vacuum material tank is provided with head tank shower, the head tank vacuum orifice of described vacuum material tank top is connected with described pumped vacuum systems, the outlet of raw material oil pipe is connected with the entrance of described head tank shower, the head tank oil outlet of described vacuum material pot bottom is connected with the entrance of crude oil pump, described crude oil pump outlet is connected with the stock oil import of vegetables oil interchanger, the material oil outlet of described vegetables oil interchanger is connected with the entrance of the distillation tower oil inlet pipe of secondary distillation tower, the distillation tower oil outlet of described secondary distillation tower bottom is connected with the depickling oil inlet of vegetables oil interchanger through depickling oil pump, the depickling oil export of described vegetables oil interchanger is connected with depickling oil tank, the overhead fraction vapour outlet of described secondary distillation tower is connected with the low boiler cut steam-in of described condensation recovering device, the middle part end vapors outlet of described secondary distillation tower is connected with the high boiling fraction steam-in of described condensation recovering device, and the withdrawer steam outlet of described condensation recovering device is connected with described pumped vacuum systems.
As preferred version of the present invention, described overhead fraction vapour outlet is positioned at the top center of described secondary distillation tower, top oil removing foam device is provided with immediately below described overhead fraction vapour outlet, the below of described top oil removing foam device is provided with top heating tank, the inwall that described top heating tank is fixed on described secondary distillation tower circumferentially and open top, below the pasta of described top heating tank is inserted in the outlet of described distillation tower oil inlet pipe, upper portion heater and top upflow tube is provided with in the heating tank of described top, the bottom of described top heating tank is provided with top and stirs vapour pipe, the lower end of described top upflow tube is passed the diapire of described top heating tank and is connected with the entrance of top oil dispenser, the below of described top oil dispenser is provided with packing layer, the below of described upper packing layer is provided with the oil-collecting annular groove be fixed on described secondary distillation inner wall of tower, is provided with gear liquid cover above the centre hole of described oil-collecting annular groove, the bottom of described oil-collecting annular groove is connected with oil-collecting annular groove oil outlet pipe, below the pasta of middle part heating tank is inserted in the lower end of described oil-collecting annular groove oil outlet pipe, middle part well heater and middle part upflow tube is provided with in the heating tank of described middle part, the bottom of described middle part heating tank is provided with middle part and stirs vapour pipe, the lower end of described middle part upflow tube through described middle part heating tank diapire and below the pasta inserting middle part oil pooling dipper, the outlet of described middle part oil pooling dipper is connected with the entrance of middle part oil dispenser, and the below of described middle part oil dispenser is provided with lower packing layer, be provided with middle part oil removing foam device between described middle part oil pooling dipper and described middle part heating tank, end vapors outlet in described middle part is between described middle part oil removing foam device and described middle part heating tank, the bottom of described secondary distillation tower is provided with bottom and stirs vapour pipe.Vegetables oil after vacuum outgas enters the heating tank of top from the distillation tower oil inlet pipe of secondary distillation tower, repeatedly baffling in the heating tank of top, and be subject to the violent stirring that the open steam that vapour pipe sprays is stirred on top, under the heating of upper portion heater, oil temperature flows out from top upflow tube to underflow stream after being elevated to setting technological temperature, after top oil dispenser distributes, even spread is in upper packing layer, full regression gas-to-liquid contact is carried out with the stirring steam in the heating tank of middle part in upper packing layer, low boiler cut in vegetables oil constantly evaporates under water vapor acting, under the suction of vacuum power source, low boiler cut steam flows upward, after the foam removal of top oil removing foam device, flow out from the overhead fraction vapour outlet at secondary distillation top of tower center, vegetables oil through one-level distillation falls into oil-collecting annular groove after upper packing layer spills, flow into the heating tank of middle part from oil-collecting annular groove oil outlet pipe again, repeatedly baffling in the heating tank of middle part, and be subject to the violent stirring that the open steam that vapour pipe sprays is stirred at middle part, under the heating of middle part well heater, after oil temperature continues rising, enter middle part oil pooling dipper from middle part upflow tube to underflow stream, middle part oil pooling dipper plays the effect of fluid-tight between the top and middle part of secondary distillation tower, after vegetables oil flows out from middle part oil pooling dipper, after middle part oil dispenser distributes, even spread is in lower packing layer, in lower packing layer, stir the stirring steam that vapour pipe sprays with bottom carry out full regression gas-to-liquid contact, high boiling fraction in vegetables oil constantly evaporates under water vapor acting, under the suction of vacuum power source, high boiling fraction steam flows upward, after the foam removal of middle part oil removing foam device, flow out from the middle part end vapors outlet of secondary distillation tower.Vegetables oil after secondary distillation falls into the bottom of secondary distillation tower, flows out from distillation tower oil outlet.
As the further preferred version of the present invention, the venting area of described top oil removing foam device and described middle part oil removing foam device central upper portion is respectively equipped with many folding waveform liquid barriers, the lower end periphery of described many folding waveform liquid barriers is connected to ring-type catch tray, and the excircle of described ring-type catch tray is downward-sloping and be connected on the inwall of described secondary distillation tower; The drop that the lower edge of each described many folding waveform liquid barriers is respectively equipped with the described ring-type catch tray that to be led by drop collects bar, and the lowest part of described ring-type catch tray is respectively equipped with outage.Low boiler cut vapour stream is when many foldings waveform liquid barrier of top oil removing foam device, high boiling fraction vapour stream is when many foldings waveform liquid barrier of middle part oil removing foam device, drop is stopped respectively, collect bar by drop and flow into ring-type catch tray, then flow out downwards from the outage of ring-type catch tray lowest part along the barrel of secondary distillation tower.
As the further preferred version of the present invention, be provided with upper wall stream below the ring-type catch tray of described top oil removing foam device and collect ring, be provided with mesospore stream between described top heating tank and described top oil dispenser and collect ring, the lowest part that described upper wall stream collects ring is connected with thrust-augmenting nozzle, and mesospore stream described in the lower end aligned of described thrust-augmenting nozzle collects ring, be provided with lower wall stream below the ring-type catch tray of described middle part oil removing foam device and collect ring, the lowest part that described mesospore stream collects ring and described lower wall stream collection ring is respectively equipped with condensate stream outlet, it is outer and be connected with condensate collector tube respectively that the external end head of described condensate stream outlet stretches out the cylindrical shell of described secondary distillation tower respectively, the outlet of described condensate collector tube is connected with the entrance of phlegma inlet valve, the outlet of described phlegma inlet valve is connected with the top fluid inlet of condensed fluid collection tank, the bottom of described condensed fluid collection tank is provided with condensate outlet valve, the outlet of described condensate outlet valve is connected with the head tank fluid infusion mouth of described vacuum material tank upper portion side wall, the top of described condensed fluid collection tank is also connected with condensed fluid collection tank steam valve, the entrance of described condensed fluid collection tank steam valve is connected with steam-pipe.
The backflow 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 flows into mesospore stream collection ring downwards from thrust-augmenting nozzle, then enters condensate collector tube from the condensate stream outlet of mesospore stream collection ring; The backflow drop of the middle part oil removing foam device therefrom outage of portion's ring-type catch tray flows into lower wall stream and collects ring, then enters condensate collector tube from the condensate stream outlet that lower wall stream collects ring; Backflow drop flows downward along condensate collector tube, enters condensed fluid collection tank from phlegma inlet valve.When condensed fluid collection tank reaches certain liquid level, close phlegma inlet valve, open condensed fluid collection tank steam valve and condensate outlet valve simultaneously, under the suction function of vapor pressure and pumped vacuum systems, namely phlegma enters vacuum material tank from head tank fluid infusion mouth and is able to reuse, and inclusion of air can be avoided in vacuum deacidification system.
As the further preferred version of the present invention, the end vapors connecting tube between described secondary distillation tower and described condensation recovering device is more and more lower along air flow line.Part end vapors touches colder duct wall and is directly condensed into liquid state, along connecting tube outwardly, enters condensation recovering device, avoids flowing back to distillation tower.
As preferred version of the present invention, described condensation recovering device is tube and shell heat exchanger, and the upper/lower terminal of described condensation recovering device is provided with upper and lower tube sheet, is connected with many water coolant tubulations between upper tubesheet and lower tubesheet; Upper and lower tube sheet is externally connected with upper and lower end socket, and the inner chamber of upper and lower end socket is left and right hydroecium by end socket baffle for separating respectively, and described lower cover is provided with withdrawer entrance of cooling water, and described upper cover is provided with withdrawer cooling water outlet; The cylinder lumen of described condensation recovering device is divided into left and right air chamber with central partition plate and the top of left and right air chamber communicates; Described high boiling fraction steam-in is connected to the bottom of described left air chamber, and the bottom of described left air chamber is provided with high boiling fraction outlet, and described high boiling fraction outlet is connected with the entrance of high boiling fraction storage tank; Described low boiler cut steam-in is connected to the bottom of described right air chamber, the upper end of described right air chamber is provided with described withdrawer steam outlet, the bottom of described right air chamber is provided with low boiler cut outlet, and described low boiler cut outlet is connected with the entrance of low boiler cut storage tank.Water coolant enters the left and right hydroecium of lower cover respectively from withdrawer entrance of cooling water, upwards flow along respective water coolant tubulation, then enters the left and right hydroecium of upper cover, finally flows out from withdrawer cooling water outlet respectively.According to the difference of different sorts cut boiling point, by regulating the cooler-water temperature of left and right hydroecium, low boiler cut and high boiling fraction are condensed respectively.The low boiler cut steam flowed out from the overhead fraction vapour outlet of secondary distillation tower enters the right air chamber of condensation recovering device from low boiler cut steam-in, in flow process from bottom to top, indirect heat exchange is carried out with water coolant, low boiler cut steam is condensed into liquid state, discharge from low boiler cut outlet, enter low boiler cut storage tank.The high boiling fraction steam flowed out from the middle part end vapors outlet of secondary distillation tower enters the left air chamber of condensation recovering device from high boiling fraction steam-in, in flow process from bottom to top, indirect heat exchange is carried out with water coolant, high boiling fraction steam is condensed into liquid state, discharge from high boiling fraction outlet, enter high boiling fraction storage tank.The residue cut lipid acid steam be not condensed, discharges from the withdrawer steam outlet of right air chamber upper end, enters lipid acid trap and proceeds trapping.
As the further preferred version of the present invention, described withdrawer steam outlet is connected with the trap inlet mouth of lipid acid trap sidewall, the inner chamber top of described lipid acid trap is provided with trap Despumation device, the below of described trap Despumation device is provided with trap shower, the below of described trap shower is provided with trap packing layer, described trap inlet mouth is positioned at the below of described trap packing layer, the top of described lipid acid trap is provided with trap bleeding point, described trap bleeding point is connected with pumped vacuum systems, the bottom of described lipid acid trap is provided with the outlet of trap lipid acid, described trap lipid acid outlet is connected with the entrance of lipid acid pump, described lipid acid pump outlet is connected with the entrance of fatty acid cycle valve with lipid acid bleed valve respectively, the outlet of described fatty acid cycle valve is connected with fatty acid cycle pipe, the outlet of described fatty acid cycle pipe is connected with the entrance of described trap shower, the outlet of described lipid acid bleed valve is connected with the entrance of lipid acid storage tank.The lipid acid steam of withdrawer condensation of not being condensed enters lipid acid trap from trap inlet mouth, from bottom to top through trap packing layer, with spray and under low temperature fatty acid liquid carry out sufficient vapour-liquid and contact, the lipid acid steam of direct condensation of residual, the trap packing layer of ordered structure provides great vapour-liquid contact area, lipid acid steam is here trapped completely, the water vapor be not condensed and air are removed after the drop carried secretly through Despumation device, be evacuated system extract out from trap bleeding point.Fall into the fatty acid liquid of lipid acid trap bottom, pumped after heat exchange cooling by lipid acid pump, enter trap shower through fatty acid cycle valve and fatty acid cycle pipe, carry out circulated sprinkling.When the lipid acid of trapping gets more and more, when the lipid acid liquid level of lipid acid trap bottom is elevated to a setting high position, opens lipid acid bleed valve, lipid acid is sent into lipid acid storage tank.
As the further preferred version of the present invention, described lipid acid pump outlet is connected with the lipid acid interchanger lipid acid entrance of lipid acid interchanger, and the lipid acid interchanger lipid acid outlet of described lipid acid interchanger is connected with the entrance of described fatty acid cycle valve; The lipid acid interchanger cooling water inlet of described lipid acid interchanger is connected with cooling water inlet pipe, and the lipid acid interchanger cooling water outlet of described lipid acid interchanger is connected with cooling water outlet pipe.The fatty acid liquid that lipid acid pump pumps, the cold side of lipid acid interchanger is first entered from lipid acid interchanger lipid acid entrance, after carrying out heat exchange with the water coolant of heat absorbing side, flow out from the outlet of lipid acid interchanger lipid acid, fatty acid cycle pipe is entered again from fatty acid cycle valve, after lipid acid is cooled, advantageously in trapping lipid acid steam.
Accompanying drawing explanation
Below in conjunction with the drawings and specific embodiments, the present invention is further detailed explanation, and accompanying drawing only provides reference and explanation use, is not used to limit the present invention.
Fig. 1 is the depickling of high valent acid vegetable oil of the present invention and the schema of cut recovery method.
Fig. 2 is the structural representation of secondary distillation tower in Fig. 1.
Fig. 3 is the enlarged view of aminoacyl site in Fig. 2.
Fig. 4 is the structural representation of condensation recovering device in Fig. 1.
Fig. 5 is the structural representation of lipid acid trap in Fig. 1.
Fig. 6 is the middle part well heater in Fig. 2 is the stereographic map of electric heating tube.
Fig. 7 is the middle part well heater in Fig. 2 is the stereographic map of hotline heater.
Fig. 8 is the middle part well heater in Fig. 2 is the stereographic map of steam heater.
In figure: 1. secondary distillation tower; 1a. distillation tower oil inlet pipe; 1b. overhead fraction vapour outlet; End vapors outlet in the middle part of 1c.; 1d. distillation tower oil outlet; 1e, 1f. condensate stream exports; Vapour pipe is stirred bottom 1g.; 2. top oil removing foam device; 2a. many foldings waveform liquid barrier; 2b. drop collects bar; 2c. ring-type catch tray; 3. top heating tank; 3a. upper portion heater; 3b. top upflow tube; Vapour pipe is stirred on 3c. top; 4. top oil dispenser; 5. go up packing layer; 6. oil-collecting annular groove; 7. keep off liquid cover; 8. oil-collecting annular groove oil outlet pipe; 9. heating tank in the middle part of; Well heater in the middle part of 9a.; Upflow tube in the middle part of 9b.; Vapour pipe is stirred in the middle part of 9c.; 10. oil pooling dipper in the middle part of; Oil dispenser in the middle part of in the of 11.; 12. times packing layers; Oil removing foam device in the middle part of in the of 13.; 14a. upper wall stream collects ring; 14a1. thrust-augmenting nozzle; 14b. mesospore stream collects ring; 14c. lower wall stream collects ring; 15. depickling oil tanks; 16. vacuum material tanks; 16a. head tank shower; 16b. head tank oil outlet; 16c. head tank vacuum orifice; 16d. head tank fluid infusion mouth; 17. condensed fluid collection tanks; 17a. phlegma inlet valve; 17b. condensate outlet valve; 17c. condensed fluid collection tank steam valve; 18. condensation recovering devices; 18a. water coolant tubulation; 18b. low boiler cut steam-in; 18c. high boiling fraction steam-in; 18d. withdrawer steam outlet; 18e. withdrawer entrance of cooling water; 18f. withdrawer cooling water outlet; 18g. end socket dividing plate; 18h. central partition plate; 18j. low boiler cut exports; 18k. high boiling fraction exports; 19. low boiler cut storage tanks; 20. high boiling fraction storage tanks; 21. lipid acid traps; 21a. trap inlet mouth; 21b. trap shower; 21c. trap packing layer; 21d. trap bleeding point; 21e. trap lipid acid exports; 21g. trap Despumation device; 21h. trap liquidometer; 22. lipid acid storage tanks; 23. lipid acid interchanger; 23a. lipid acid interchanger lipid acid entrance; 23b. lipid acid interchanger lipid acid exports; 24. fatty acid cycle valves; 25. lipid acid bleed valves; 26. vegetables oil interchanger.G1. raw material oil pipe; G2. steam-pipe; G3. condensate collector tube; G4. fatty acid cycle pipe; G5. cooling water inlet pipe; G6. cooling water outlet pipe; B1. crude oil pump; B2. depickling oil pump; B3. lipid acid pump.
Embodiment
As shown in Figure 1, depickling and the cut recovery method of high valent acid vegetable oil of the present invention in turn include the following steps: the stock oil of 100 ± 5 DEG C enters in vacuum material tank 16 and sprays, remove the moisture and air that dissolve in stock oil, mentioned component is avoided to have a negative impact to oil product when high temperature depickling, absolute pressure in vacuum material tank 16 is 2mbar, then the high temperature depickling oil of stock oil and 225 ± 5 DEG C carries out indirect heat exchange, stock oil enters after being warming up to 190 ± 5 DEG C in secondary distillation tower 1 again and carries out the first step successively and add thermal distillation and the second stage adds thermal distillation, after first step heating, oil temperature rises to 220 ± 5 DEG C, after the heating of the second stage, oil temperature rises to 240 ± 5 DEG C, the high temperature depickling oil of described 225 ± 5 DEG C is become after two-step heating distillation, after described high temperature depickling oil and described stock oil indirect heat exchange, temperature is reduced to 135 ± 5 DEG C and is entered depickling oil tank.
The first step adds the low boiler cut steam of 115 ± 5 DEG C that thermal distillation produces and enters condensation recovering device 18 from low boiler cut steam-in and be cooled after water indirect condensing becomes liquid state, enter low boiler cut storage tank 19, cooling water inlet temperature is 50 DEG C, and cooling water outlet temperature is 55 DEG C.
The second stage adds the high boiling fraction steam of 125 ± 5 DEG C that thermal distillation produces and enters condensation recovering device 18 from high boiling fraction steam-in and be cooled after water indirect condensing becomes liquid state, enter high boiling fraction storage tank 20, cooling water inlet temperature is 55 DEG C, and cooling water outlet temperature is 60 DEG C.
In secondary distillation tower 1, the first step adds the absolute pressure that the steam outlet of thermal distillation and the second stage adds the steam outlet of thermal distillation and is 2mbar.
The residue lipid acid vapor temperature be not condensed in cut is 80 DEG C, lipid acid trap 21 is escaped and enter from the withdrawer steam outlet 18d on condensation recovering device 18 top, in lipid acid trap 21, the low temperature fatty acid liquid of 50 DEG C carries out circulated sprinkling trapping to lipid acid steam, the fatty acid liquid temperature fallen into bottom lipid acid trap 21 is 60 DEG C, after being pumped by lipid acid pump B3, the top getting back to described lipid acid trap 21 after water coolant is lowered the temperature indirectly sprays, cooling water inlet temperature is 32 DEG C, and cooling water outlet temperature is 37 DEG C; The top of described lipid acid trap 21 is connected with pumped vacuum systems, and the absolute pressure in lipid acid trap 21 is 1.5mbar.
The inner chamber top of vacuum material tank 16 is provided with head tank shower 16a, the head tank vacuum orifice 16c at vacuum material tank 16 top is connected with pumped vacuum systems, the outlet of raw material oil pipe G1 is connected with the entrance of head tank shower 16a, head tank oil outlet 16b bottom vacuum material tank 16 is connected with the entrance of crude oil pump B1, the outlet of crude oil pump B1 is connected with the stock oil import of vegetables oil interchanger 26, the material oil outlet of vegetables oil interchanger 26 is connected with the entrance of the distillation tower oil inlet pipe of secondary distillation tower 1, distillation tower oil outlet 1d bottom secondary distillation tower 1 is connected with the depickling oil inlet of vegetables oil interchanger 26 through depickling oil pump B2, the depickling oil export of vegetables oil interchanger 26 is connected with depickling oil tank 15.
The overhead fraction vapour outlet 1b of secondary distillation tower 1 is connected with the low boiler cut steam-in 18b of condensation recovering device 18, and the middle part end vapors outlet 1c of secondary distillation tower 1 is connected with the high boiling fraction steam-in 18c of condensation recovering device 18.End vapors connecting tube between secondary distillation tower 1 and condensation recovering device 18 is more and more lower along air flow line.Part end vapors touches colder duct wall and is directly condensed into liquid state, along connecting tube outwardly, enters condensation recovering device 18, avoids flowing back to distillation tower 1.
Pumped vacuum systems is undertaken aspirating by head tank vacuum orifice 16c makes the inner chamber of vacuum material tank 16 be in vacuum state, and the high valent acid vegetable oil that former process is come sprays through raw material oil pipe G1 incoming stock tank shower 16a.Vegetables oil after vacuum outgas flows out from the head tank oil outlet 16b bottom vacuum material tank 16, send into vegetables oil interchanger 26 by crude oil pump B1 and carry out indirect heat exchange with the depickling oil of high temperature, the oil temperature of depickling oil declines, the oil temperature of stock oil raises, then stock oil flows out from the material oil outlet of vegetables oil interchanger 26, enter the distillation tower oil inlet pipe 1a of secondary distillation tower 1, first through low-temperature distillation, the low boiler cut in vegetables oil is evaporated in secondary distillation tower 1, then through pyrogenic distillation, the high boiling fraction in vegetables oil is evaporated; Low boiler cut steam is discharged from the overhead fraction vapour outlet 1b of secondary distillation tower 1, enters condensation recovering device 18 condensation from low boiler cut steam-in 18b; High boiling fraction steam is discharged from the middle part end vapors outlet 1c of secondary distillation tower 1, and enter condensation recovering device 18 condensation from high boiling fraction steam-in 18c, the low boiler cut in vegetables oil and high boiling fraction are able to be separated from vegetables oil respectively.
Depickling oil after secondary depickling flows out from the distillation tower oil outlet 1d bottom secondary distillation tower 1, the depickling oil inlet of vegetables oil interchanger 26 is pumped into by depickling oil pump B2, after carrying out preheating to stock oil, depickling oil flows out from the depickling oil export of vegetables oil interchanger 26, enters depickling oil tank 15.
As shown in Figure 2, overhead fraction vapour outlet 1b is positioned at the top center of secondary distillation tower 1, top oil removing foam device 2 is provided with immediately below overhead fraction vapour outlet 1b, the below of top oil removing foam device 2 is provided with top heating tank 3, the inwall that top heating tank 3 is fixed on secondary distillation tower 1 circumferentially and open top, below the pasta of top heating tank 3 is inserted in the outlet of distillation tower oil inlet pipe 1a, upper portion heater 3a and top upflow tube 3b is provided with in top heating tank 3, the bottom of top heating tank 3 is provided with top and stirs vapour pipe 3c, the lower end of top upflow tube 3b is passed the diapire of top heating tank 3 and is connected with the entrance of top oil dispenser 4, the below of top oil dispenser 4 is provided with packing layer 5, the below of upper packing layer 5 is provided with the oil-collecting annular groove 6 be fixed on secondary distillation tower 1 inwall, is provided with gear liquid cover 7 above the centre hole of oil-collecting annular groove 6, the bottom of oil-collecting annular groove 6 is connected with oil-collecting annular groove oil outlet pipe 8, below the pasta of middle part heating tank 9 is inserted in the lower end of oil-collecting annular groove oil outlet pipe 8, middle part well heater 9a and middle part upflow tube 9b is provided with in the heating tank 9 of middle part, the bottom of middle part heating tank 9 is provided with middle part and stirs vapour pipe 9c, the lower end of middle part upflow tube 9b through middle part heating tank 9 diapire and below the pasta inserting middle part oil pooling dipper 10, the outlet of middle part oil pooling dipper 10 is connected with the entrance of middle part oil dispenser 11, and the below of middle part oil dispenser 11 is provided with lower packing layer 12, be provided with middle part oil removing foam device 13 between middle part oil pooling dipper 10 and middle part heating tank 9,1c is between middle part oil removing foam device 13 and middle part heating tank 9 for the outlet of middle part end vapors, the bottom of secondary distillation tower 1 is provided with bottom and stirs vapour pipe 1g.
Vegetables oil after vacuum outgas enters top heating tank 3 from the distillation tower oil inlet pipe 1a of secondary distillation tower 1, repeatedly baffling in top heating tank 3, and be subject to the violent stirring that the open steam that vapour pipe 3c sprays is stirred on top, under the heating of upper portion heater 3a, oil temperature flows out from top upflow tube 3b to underflow stream after being elevated to setting technological temperature, after top oil dispenser 4 distributes, even spread is in upper packing layer 5, full regression gas-to-liquid contact is carried out with the stirring steam in middle part heating tank 9 in upper packing layer 5, low boiler cut in vegetables oil constantly evaporates under water vapor acting, under the suction of vacuum power source, low boiler cut steam flows upward, after the foam removal of top oil removing foam device 2, flow out from the overhead fraction vapour outlet 1b of secondary distillation tower 1 top center,
The vegetables oil of removing low boiler cut falls into oil-collecting annular groove 6 after upper packing layer 5 spills, flow into the heating tank 9 of middle part from oil-collecting annular groove oil outlet pipe 8 again, repeatedly baffling in middle part heating tank 9, and be subject to the violent stirring that the open steam that vapour pipe 9c sprays is stirred at middle part, under the heating of middle part well heater 9a, after oil temperature continues rising, enter middle part oil pooling dipper 10 from middle part upflow tube 9b to underflow stream, middle part oil pooling dipper 10 plays the effect of fluid-tight between the top and middle part of secondary distillation tower 1, after vegetables oil flows out from middle part oil pooling dipper 10, after middle part oil dispenser 11 distributes, even spread is in lower packing layer 12, in lower packing layer 12, stir the stirring steam that vapour pipe 1g sprays with bottom carry out full regression gas-to-liquid contact, high boiling fraction in vegetables oil constantly evaporates under water vapor acting, under the suction of vacuum power source, high boiling fraction steam flows upward, after the foam removal of middle part oil removing foam device 13, flow out from the middle part end vapors outlet 1c of secondary distillation tower 1.
Vegetables oil after secondary distillation falls into the bottom of secondary distillation tower 1, flows out from distillation tower oil outlet 1d.
As shown in Figures 2 and 3, the venting area of top oil removing foam device 2 and middle part oil removing foam device 13 central upper portion is respectively equipped with many folding waveform liquid barrier 2a, the lower end periphery of many foldings waveform liquid barrier 2a is connected to ring-type catch tray 2c, and the excircle of ring-type catch tray 2c is downward-sloping and be connected on the inwall of secondary distillation tower 1; The drop that the lower edge of each many folding waveform liquid barrier 2a is respectively equipped with the ring-type catch tray 2c that to be led by drop collects bar 2b, and the lowest part of ring-type catch tray 2c is respectively equipped with outage.
Low boiler cut vapour stream is when many foldings waveform liquid barrier 2a of top oil removing foam device 2, high boiling fraction vapour stream is when many foldings waveform liquid barrier of middle part oil removing foam device 13, drop is stopped respectively, collect bar 2b by drop and flow into ring-type catch tray 2c, then flow out downwards from the outage of ring-type catch tray 2c lowest part along the barrel of secondary distillation tower 1.
Be provided with upper wall stream below the ring-type catch tray 2c of top oil removing foam device 2 and collect ring 14a, be provided with mesospore stream between top heating tank 3 and top oil dispenser 4 and collect ring 14b, the lowest part that upper wall stream collects ring 14a is connected with thrust-augmenting nozzle 14a1, and the lower end aligned mesospore stream of thrust-augmenting nozzle 14a1 collects ring 14b, be provided with lower wall stream below the ring-type catch tray of middle part oil removing foam device 13 and collect ring 14c, the lowest part that mesospore stream collects ring 14b is provided with condensate stream outlet 1e, the lowest part that lower wall stream collects ring 14c is provided with condensate stream outlet 1f, it is outer and be connected with condensate collector tube G3 respectively that the external end head of condensate stream outlet 1e and condensate stream outlet 1f stretches out the cylindrical shell of secondary distillation tower 1 respectively, the outlet of condensate collector tube G3 is connected with the entrance of phlegma inlet valve 17a, the outlet of phlegma inlet valve 17a is connected with the top fluid inlet of condensed fluid collection tank 17, the bottom of condensed fluid collection tank 17 is provided with condensate outlet valve 17b, the outlet of condensate outlet valve 17b is connected with the head tank fluid infusion mouth 16d of vacuum material tank 16 upper portion side wall, the top of condensed fluid collection tank 17 is also connected with condensed fluid collection tank steam valve 17c, the entrance of condensed fluid collection tank steam valve 17c is connected with steam-pipe G2.
The backflow 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, flow into mesospore stream downwards from thrust-augmenting nozzle 14a1 again and collect ring 14b, then enter condensate collector tube G3 from the condensate stream outlet 1e of mesospore stream collection ring 14b; The backflow drop of the middle part oil removing foam device 13 therefrom outage of portion's ring-type catch tray flows into lower wall stream and collects ring 14c, then enters condensate collector tube G3 from the condensate stream outlet 1f that lower wall stream collects ring 14c; Backflow drop flows downward along condensate collector tube G3, enters condensed fluid collection tank 17 from phlegma inlet valve 17a.When condensed fluid collection tank 17 reaches certain liquid level, close phlegma inlet valve 17a, open condensed fluid collection tank steam valve 17c and condensate outlet valve 17b simultaneously, under the suction function of vapor pressure and pumped vacuum systems, namely phlegma enters vacuum material tank 16 from head tank fluid infusion mouth 16d and is able to reuse, and inclusion of air can be avoided in vacuum deacidification system.
As shown in Figure 6 to 8, middle part well heater 9a can be electric heater, hotline heater and steam heater, and upper portion heater 3a is also like this.According to different oil products and processing requirement, different well heaters can be selected.
As shown in Figure 4, condensation recovering device 18 is tube and shell heat exchanger, and the upper/lower terminal of condensation recovering device 18 is provided with upper and lower tube sheet, is connected with many water coolant tubulation 18a between upper tubesheet and lower tubesheet; Upper and lower tube sheet is externally connected with upper and lower end socket, and the inner chamber of upper and lower end socket is divided into left and right hydroecium by end socket dividing plate 18g respectively, and lower cover is provided with withdrawer entrance of cooling water 18e, and upper cover is provided with withdrawer cooling water outlet 18f; The cylinder lumen of condensation recovering device 18 is divided into left and right air chamber to central partition plate 18h and the top of left and right air chamber communicates; High boiling fraction steam-in 18c is connected to the bottom of left air chamber, and the bottom of left air chamber is provided with high boiling fraction outlet 18k, and high boiling fraction outlet 18k is connected with the entrance of high boiling fraction storage tank 20; Low boiler cut steam-in 18b is connected to the bottom of right air chamber, and the upper end of right air chamber is provided with withdrawer steam outlet 18d, and the bottom of right air chamber is provided with low boiler cut outlet 18j, and low boiler cut outlet 18j is connected with the entrance of low boiler cut storage tank 19.
Water coolant enters the left and right hydroecium of lower cover respectively from withdrawer entrance of cooling water 18e, upwards flow, then enter the left and right hydroecium of upper cover along respective water coolant tubulation 18a, finally flows out from withdrawer cooling water outlet 18f respectively.According to the difference of different sorts cut boiling point, by regulating the cooler-water temperature of left and right hydroecium, low boiler cut and high boiling fraction are condensed respectively.
The low boiler cut steam flowed out from the overhead fraction vapour outlet 1b of secondary distillation tower 1 enters the right air chamber of condensation recovering device 18 from low boiler cut steam-in 18b, in flow process from bottom to top, indirect heat exchange is carried out with water coolant, low boiler cut steam is condensed into liquid state, discharge from low boiler cut outlet 18j, enter low boiler cut storage tank 19.
The high boiling fraction steam flowed out from the middle part end vapors outlet 1c of secondary distillation tower 1 enters the left air chamber of condensation recovering device 18 from high boiling fraction steam-in 18c, in flow process from bottom to top, indirect heat exchange is carried out with water coolant, high boiling fraction steam is condensed into liquid state, discharge from high boiling fraction outlet 18k, enter high boiling fraction storage tank 20.
The residue end vapors be not condensed, is mainly lipid acid steam, discharges from the withdrawer steam outlet 18d of right air chamber upper end, enters lipid acid trap 21 and proceeds trapping.
As shown in Figure 5, withdrawer steam outlet 18d is connected with the trap inlet mouth 21a of lipid acid trap 21 sidewall, the inner chamber top of lipid acid trap 21 is provided with trap Despumation device 21g, the below of trap Despumation device 21g is provided with trap shower 21b, the below of trap shower 21b is provided with trap packing layer 21c, trap inlet mouth 21a is positioned at the below of trap packing layer 21c, the top of lipid acid trap 21 is provided with trap bleeding point 21d, trap bleeding point 21d is connected with pumped vacuum systems, the bottom of lipid acid trap 21 is provided with trap lipid acid outlet 21e, trap lipid acid outlet 21e is connected with the entrance of lipid acid pump B3, the outlet of lipid acid pump B3 is connected with the entrance of fatty acid cycle valve 24 with lipid acid bleed valve 25 respectively, the outlet of fatty acid cycle valve 24 is connected with fatty acid cycle pipe G4, the outlet of fatty acid cycle pipe G4 is connected with the entrance of trap shower 21b, the outlet of lipid acid bleed valve 25 is connected with the entrance of lipid acid storage tank 22.The bottom of lipid acid trap 21 is provided with trap liquidometer 21h.
The lipid acid steam of withdrawer 18 condensation of not being condensed enters lipid acid trap 21 from trap inlet mouth 21a, 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, the lipid acid steam of direct condensation of residual, the trap packing layer 21c of ordered structure provides great vapour-liquid contact area, lipid acid steam is here trapped completely, the water vapor be not condensed and air are removed after the drop carried secretly through Despumation device, be evacuated system extract out from trap bleeding point 21d.Fall into the fatty acid liquid bottom lipid acid trap 21, pumped by lipid acid pump B3, enter trap shower 21b through fatty acid cycle valve 24 and fatty acid cycle pipe G4, carry out circulated sprinkling.When the lipid acid of trapping gets more and more, when trap liquidometer 21h detects a setting high position, Controlling System opens lipid acid bleed valve 25, lipid acid is sent into lipid acid storage tank 22.
As shown in Figure 1, the outlet of lipid acid pump B3 is connected with the lipid acid interchanger lipid acid entrance 23a of lipid acid interchanger 23, and the lipid acid interchanger lipid acid outlet 23b of lipid acid interchanger 23 is connected with the entrance of fatty acid cycle valve 24; The lipid acid interchanger cooling water inlet of lipid acid interchanger 23 is connected with cooling water inlet pipe G5, and the lipid acid interchanger cooling water outlet of lipid acid interchanger 23 is connected with cooling water outlet pipe G6.
The fatty acid liquid that lipid acid pump B3 pumps, the cold side of lipid acid interchanger is first entered from lipid acid interchanger lipid acid entrance 23a, after carrying out heat exchange with the water coolant of heat absorbing side, flow out from lipid acid interchanger lipid acid outlet 23b, fatty acid cycle pipe G4 is entered again from fatty acid cycle valve 24, after lipid acid is cooled, advantageously in trapping lipid acid steam, the heat in lipid acid can be reclaimed simultaneously.
The foregoing is only the better possible embodiments of the present invention, non-ly therefore limit to scope of patent protection of the present invention.In addition to the implementation, the present invention can also have other embodiments.All employings are equal to the technical scheme of replacement or equivalent transformation formation, all drop in the protection domain of application claims.The present invention can pass through without the technical characteristic described or adopt existing techniques in realizing, does not repeat them here.
Claims (10)
1. the depickling of a high valent acid vegetable oil and cut recovery method, it is characterized in that, in turn include the following steps: stock oil enters in vacuum material tank and sprays, remove the moisture and air that dissolve in stock oil, then stock oil and high temperature depickling oil carry out indirect heat exchange, stock oil enters in secondary distillation tower after heating up again and carries out the first step successively and add thermal distillation and the second stage adds thermal distillation, become described high temperature depickling oil after two-step heating distillation, after described high temperature depickling oil and described stock oil indirect heat exchange, enter depickling oil tank; The first step adds low boiler cut steam that thermal distillation produces and enters condensation recovering device from low boiler cut steam-in and be cooled after water indirect condensing becomes liquid state, enters low boiler cut storage tank; The second stage adds high boiling fraction steam that thermal distillation produces and enters condensation recovering device from high boiling fraction steam-in and be cooled after water indirect condensing becomes liquid state, enters high boiling fraction storage tank; The residue lipid acid steam be not condensed in cut, lipid acid trap is escaped and enter from the withdrawer steam outlet on condensation recovering device top, in described lipid acid trap, low temperature fatty acid liquid carries out circulated sprinkling trapping to lipid acid steam, fall into the fatty acid liquid of lipid acid trap bottom, after being pumped by lipid acid pump, the top getting back to described lipid acid trap after water coolant is lowered the temperature indirectly sprays; The top of described lipid acid trap is connected with pumped vacuum systems.
2. the depickling of high valent acid vegetable oil according to claim 1 and cut recovery method, it is characterized in that: the temperature of described stock oil is 100 ± 5 DEG C, 190 ± 5 DEG C are warming up to after the heat exchange of high temperature depickling oil, after first step heating, oil temperature rises to 220 ± 5 DEG C, after the heating of the second stage, oil temperature rises to 240 ± 5 DEG C, temperature before described high temperature depickling oil and described stock oil heat exchange is 225 ± 5 DEG C, and the temperature after heat exchange is 135 ± 5 DEG C; The low boiler cut vapor temperature of described secondary distillation tower discharge is 115 ± 5 DEG C, and the high boiling fraction vapor temperature of described secondary distillation tower discharge is 125 ± 5 DEG C; The residue lipid acid vapor temperature of discharging from described condensation recovering device is 80 DEG C, and in described lipid acid trap, the spray temperature of low temperature fatty acid liquid is 50 DEG C; Absolute pressure in described lipid acid trap is 1.5mbar, and the first step in described vacuum material tank and described secondary distillation tower adds the absolute pressure that thermal distillation and the second stage adds thermal distillation and is 2mbar.
3. the depickling of high valent acid vegetable oil according to claim 1 and 2 and cut recovery method, it is characterized in that: the inner chamber top of described vacuum material tank is provided with head tank shower, the head tank vacuum orifice of described vacuum material tank top is connected with described pumped vacuum systems, the outlet of raw material oil pipe is connected with the entrance of described head tank shower, the head tank oil outlet of described vacuum material pot bottom is connected with the entrance of crude oil pump, described crude oil pump outlet is connected with the stock oil import of vegetables oil interchanger, the material oil outlet of described vegetables oil interchanger is connected with the entrance of the distillation tower oil inlet pipe of secondary distillation tower, the distillation tower oil outlet of described secondary distillation tower bottom is connected with the depickling oil inlet of vegetables oil interchanger through depickling oil pump, the depickling oil export of described vegetables oil interchanger is connected with depickling oil tank, the overhead fraction vapour outlet of described secondary distillation tower is connected with the low boiler cut steam-in of described condensation recovering device, the middle part end vapors outlet of described secondary distillation tower is connected with the high boiling fraction steam-in of described condensation recovering device, and the withdrawer steam outlet of described condensation recovering device is connected with described pumped vacuum systems.
4. the depickling of high valent acid vegetable oil according to claim 3 and cut recovery method, it is characterized in that: described overhead fraction vapour outlet is positioned at the top center of described secondary distillation tower, top oil removing foam device is provided with immediately below described overhead fraction vapour outlet, the below of described top oil removing foam device is provided with top heating tank, the inwall that described top heating tank is fixed on described secondary distillation tower circumferentially and open top, below the pasta of described top heating tank is inserted in the outlet of described distillation tower oil inlet pipe, upper portion heater and top upflow tube is provided with in the heating tank of described top, the bottom of described top heating tank is provided with top and stirs vapour pipe, the lower end of described top upflow tube is passed the diapire of described top heating tank and is connected with the entrance of top oil dispenser, the below of described top oil dispenser is provided with packing layer, the below of described upper packing layer is provided with the oil-collecting annular groove be fixed on described secondary distillation inner wall of tower, is provided with gear liquid cover above the centre hole of described oil-collecting annular groove, the bottom of described oil-collecting annular groove is connected with oil-collecting annular groove oil outlet pipe, below the pasta of middle part heating tank is inserted in the lower end of described oil-collecting annular groove oil outlet pipe, middle part well heater and middle part upflow tube is provided with in the heating tank of described middle part, the bottom of described middle part heating tank is provided with middle part and stirs vapour pipe, the lower end of described middle part upflow tube through described middle part heating tank diapire and below the pasta inserting middle part oil pooling dipper, the outlet of described middle part oil pooling dipper is connected with the entrance of middle part oil dispenser, and the below of described middle part oil dispenser is provided with lower packing layer, be provided with middle part oil removing foam device between described middle part oil pooling dipper and described middle part heating tank, end vapors outlet in described middle part is between described middle part oil removing foam device and described middle part heating tank, the bottom of described secondary distillation tower is provided with bottom and stirs vapour pipe.
5. the depickling of high valent acid vegetable oil according to claim 4 and cut recovery method, it is characterized in that: the venting area of described top oil removing foam device and described middle part oil removing foam device central upper portion is respectively equipped with many folding waveform liquid barriers, the lower end periphery of described many folding waveform liquid barriers is connected to ring-type catch tray, and the excircle of described ring-type catch tray is downward-sloping and be connected on the inwall of described secondary distillation tower; The drop that the lower edge of each described many folding waveform liquid barriers is respectively equipped with the described ring-type catch tray that to be led by drop collects bar, and the lowest part of described ring-type catch tray is respectively equipped with outage.
6. the depickling of high valent acid vegetable oil according to claim 5 and cut recovery method, it is characterized in that: be provided with upper wall stream below the ring-type catch tray of described top oil removing foam device and collect ring, be provided with mesospore stream between described top heating tank and described top oil dispenser and collect ring, the lowest part that described upper wall stream collects ring is connected with thrust-augmenting nozzle, and mesospore stream described in the lower end aligned of described thrust-augmenting nozzle collects ring, be provided with lower wall stream below the ring-type catch tray of described middle part oil removing foam device and collect ring, the lowest part that described mesospore stream collects ring and described lower wall stream collection ring is respectively equipped with condensate stream outlet, it is outer and be connected with condensate collector tube respectively that the external end head of described condensate stream outlet stretches out the cylindrical shell of described secondary distillation tower respectively, the outlet of described condensate collector tube is connected with the entrance of phlegma inlet valve, the outlet of described phlegma inlet valve is connected with the top fluid inlet of condensed fluid collection tank, the bottom of described condensed fluid collection tank is provided with condensate outlet valve, the outlet of described condensate outlet valve is connected with the head tank fluid infusion mouth of described vacuum material tank upper portion side wall, the top of described condensed fluid collection tank is also connected with condensed fluid collection tank steam valve, the entrance of described condensed fluid collection tank steam valve is connected with steam-pipe.
7. the depickling of high valent acid vegetable oil according to claim 3 and cut recovery method, is characterized in that: the end vapors connecting tube between described secondary distillation tower and described condensation recovering device is more and more lower along air flow line.
8. the depickling of high valent acid vegetable oil according to claim 1 and 2 and cut recovery method, it is characterized in that: described condensation recovering device is tube and shell heat exchanger, the upper/lower terminal of described condensation recovering device is provided with upper and lower tube sheet, is connected with many water coolant tubulations between upper tubesheet and lower tubesheet; Upper and lower tube sheet is externally connected with upper and lower end socket, and the inner chamber of upper and lower end socket is left and right hydroecium by end socket baffle for separating respectively, and described lower cover is provided with withdrawer entrance of cooling water, and described upper cover is provided with withdrawer cooling water outlet; The cylinder lumen of described condensation recovering device is divided into left and right air chamber with central partition plate and the top of left and right air chamber communicates; Described high boiling fraction steam-in is connected to the bottom of described left air chamber, and the bottom of described left air chamber is provided with high boiling fraction outlet, and described high boiling fraction outlet is connected with the entrance of high boiling fraction storage tank; Described low boiler cut steam-in is connected to the bottom of described right air chamber, the upper end of described right air chamber is provided with described withdrawer steam outlet, the bottom of described right air chamber is provided with low boiler cut outlet, and described 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 2 and cut recovery method, it is characterized in that: described withdrawer steam outlet is connected with the trap inlet mouth of lipid acid trap sidewall, the inner chamber top of described lipid acid trap is provided with trap Despumation device, the below of described trap Despumation device is provided with trap shower, the below of described trap shower is provided with trap packing layer, described trap inlet mouth is positioned at the below of described trap packing layer, the top of described lipid acid trap is provided with trap bleeding point, described trap bleeding point is connected with pumped vacuum systems, the bottom of described lipid acid trap is provided with the outlet of trap lipid acid, described trap lipid acid outlet is connected with the entrance of lipid acid pump, described lipid acid pump outlet is connected with the entrance of fatty acid cycle valve with lipid acid bleed valve respectively, the outlet of described fatty acid cycle valve is connected with fatty acid cycle pipe, the outlet of described fatty acid cycle pipe is connected with the entrance of described trap shower, the outlet of described lipid acid bleed valve is connected with the entrance of lipid acid storage tank.
10. the depickling of high valent acid vegetable oil according to claim 9 and cut recovery method, it is characterized in that: described lipid acid pump outlet is connected with the lipid acid interchanger lipid acid entrance of lipid acid interchanger, the lipid acid interchanger lipid acid outlet of described lipid acid interchanger is connected with the entrance of described fatty acid cycle valve; The lipid acid interchanger cooling water inlet of described lipid acid interchanger is connected with cooling water inlet pipe, and the lipid acid interchanger cooling water outlet of described lipid acid interchanger is connected with cooling water outlet pipe.
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| 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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