Integrated vegetable oil refining system

Abstract

The application discloses a plant oil integrated refining system, each section of which is provided with an integrated combined tower, and the integrated combined alkali refining tower is sequentially provided with a water washing buffer section, a secondary acidification reaction section and an alkali reaction section from top to bottom; the outlet of a degummed oil output pipe is connected with the main inlet of a static acid mixer through a steam heater; the outlet of the static acid mixer is connected with the secondary acidification reaction section; the outlet of the secondary acidification reaction section is connected with the main inlet of a static alkali mixer through a secondary acidification oil delivery pump; the outlet of the static alkali mixer is connected with the alkali reaction section; the outlet of the alkali reaction section is connected with a desoaping centrifuge through a neutralization oil delivery pump and a steam heater; the light phase desoaping oil outlet of the desoaping centrifuge is connected with the upper end inlet of the water washing buffer section; the bottom outlet of the water washing buffer section is connected with the inlet of a water washing centrifuge; and the light phase water washing oil outlet of the water washing centrifuge is connected with a water washing oil output pipe. The application can reduce equipment cost, save installation materials, reduce system floor area and building area.

Description

TECHNICAL FIELD

[0001] The present application relates to an oil refining system, in particular to an integrated vegetable oil refining system, and belongs to the technical field of oil refining. BACKGROUND

[0002] The oil refining plant includes a degumming section, an alkali refining section, a bleaching section, a deodorization section, and a winterization section. For the degumming section, according to the process characteristics, it is divided into water degumming, acid degumming, super degumming, and enzyme degumming. Among them: 1. Water degumming is applied to the occasion where the hydrated phospholipids in the oil are combined with process hot water to form a colloid and are separated from the oil. Water degumming is often used to produce high-quality phospholipid products; 2. Acid degumming is applied to the occasion where part of the non-hydrated phospholipids in the oil are converted into hydrated phospholipids through acidification reaction, and then combined with process hot water to form a colloid and separated from the oil. Acid degumming is often used to reduce the phospholipid content in the oil and improve the frying quality of the oil; 3. Super degumming is applied to the occasion where part of the non-hydrated phospholipids in the oil are converted into hydrated phospholipids through acidification reaction, and then combined with dilute alkali water to form a colloid and separated from the oil. Super degumming can remove most of the phospholipids in the oil and obtain high-quality degummed oil; 4. Enzymatic degumming is applied to the occasion where the non-hydrated phospholipids in the oil are reacted with enzymes, the hydrophilicity of the reacted non-hydrated phospholipids is enhanced, and then combined with process hot water to form a colloid and separated from the oil. Enzymatic degumming can remove most of the phospholipids in the oil and obtain high-quality degummed oil while improving the oil yield. The above degumming processes can be selected according to different process requirements.

[0003] A Chinese invention patent with the authorization publication number CN1042140C discloses a continuous water degumming equipment for vegetable oil, which includes a pump, a heat exchanger, a hot water tank, a multi-layer reaction tank (watering tank), a separator, a vacuum dryer, and other equipment. The above equipment is separately arranged, and the watering tank adopts paddle mechanical stirring.

[0004] A Chinese utility model patent with the publication number CN211972258U discloses a novel oil enzymatic degumming production integrated system, which includes a pump, a heat exchanger, a mixer, a centrifuge, an acid storage tank, an alkali storage tank, an acid reaction tank, an enzyme reaction tank, and other equipment. The above equipment is separately arranged and is a non-standard container type equipment. The acid reaction tank and the enzyme reaction tank adopt paddle mechanical stirring.

[0005] Traditional alkali refining section includes non-standard container devices such as acidification tank, alkali reaction tank, water washing buffer tank, vacuum dryer, soft water tank, hot water tank, in addition to pumps, heat exchangers, mixers, centrifuges and other equipment. Among them, the acidification tank, alkali reaction tank and water washing buffer tank also have mechanical stirring devices. For example, the Chinese utility model patent with publication number CN204737934U discloses an oil alkali refining device, which includes lye tank, water tank, alkali refining pot, centrifuge, oil tank, saponification pot and other equipment. The above devices are separately arranged, and the alkali refining pot and saponification pot adopt paddle type mechanical stirring.

[0006] Traditional decolorization section includes non-standard container devices such as pulse dust collector, decolorizing agent adding metering system, premix tank, decolorization tower, intermediate oil tank, in addition to pumps, heat exchangers, filters and other equipment. For example, the Chinese utility model patent with publication number CN211946944U discloses an oil decolorization system, which includes pre-decolorization tower, pre-decolorization filter, decolorization premix tank, decolorization tower, self-cleaning filter and decolorization filter. The above devices are separately arranged.

[0007] The Chinese utility model patent with publication number CN218642694U discloses an edible oil zero trans fatty acid deodorization system, which includes non-standard container devices such as gas separation chamber, energy saver, falling film heater, deodorization tower, fatty acid trap, in addition to pumps, heat exchangers and other equipment.

[0008] Traditional vegetable oil refining system and process generally have the following problems:

[0009] 1. The process design of each section is complex, the process equipment is much, the installation materials of various media such as pipes and valves are much, and a large amount of building space is needed; which significantly increases the project construction cost and increases the project construction period;

[0010] 2. Due to the large number of pipes and equipment in each section, the internal materials are difficult to be discharged in time and effectively, and a large amount of residues remain in the system, which easily causes pipe blockage and affects product quality;

[0011] 3. The paddle type mechanical stirring device is used in multiple reaction tanks of each section, the stirring and mixing efficiency is low, the reaction process is not sufficient, the consumption of acid and alkali auxiliary materials is large, the oil loss is high, and the maintenance cost is increased;

[0012] 4. The traditional decolorization section adds decolorizing agent in the form of AB valve plus metering cylinder, which is batch addition; the mechanical stirring mixing form under vacuum is used for mixing clay and oil, which leads to insufficient mixing of clay and oil, large consumption of decolorizing agent auxiliary materials, high oil loss, and the decolorizing agent is easy to enter the vacuum pipeline and vacuum equipment under vacuum, causing pipe and equipment blockage, affecting normal production, and increasing maintenance cost;

[0013] 5. In traditional deodorization processes, both energy-saving heat exchange and final heating before deodorization require a long time. The oil stays at high temperatures for an extended period, resulting in the significant loss of some nutrients in the refined oil, such as vitamin E and sterols. At the same time, the content of harmful substances, such as trans fatty acids and glycidyl esters, increases. Summary of the Invention

[0014] The purpose of this section is to outline some aspects of embodiments of the present invention and to briefly describe some preferred embodiments. Simplifications or omissions may be made in this section, as well as in the abstract and title of this application, to avoid obscuring the purpose of these documents; however, such simplifications or omissions should not be construed as limiting the scope of the invention.

[0015] In view of the problems existing in the above and / or prior art, the present invention is proposed.

[0016] The purpose of this invention is to overcome the problems existing in the prior art and provide an integrated vegetable oil refining system that replaces the traditional decentralized process reaction tanks, simplifies the refining process, reduces equipment manufacturing costs, saves installation materials, and reduces the system footprint and building area.

[0017] To solve the above technical problems, the present invention provides an integrated vegetable oil refining system, comprising a degumming section and an alkali refining section. The alkali refining section includes an integrated combined alkali refining tower, which comprises a water washing buffer section, a secondary acidification reaction section, and an alkali reaction section stacked sequentially from top to bottom. The outlet of the degummed oil output pipe is connected to the cold side inlet of steam heater C. The cold side outlet of steam heater C is connected to the main inlet of static acid mixer B. The outlet of static acid mixer B is connected to the top inlet of the secondary acidification reaction section. The bottom outlet of the secondary acidification reaction section is connected to... The secondary acidification oil transfer pump is connected to the main inlet of the static alkali mixer B. The outlet of the static alkali mixer B is connected to the upper inlet of the alkali reaction section. The bottom outlet of the alkali reaction section is connected to the cold side inlet of the steam heater D via the neutralization oil transfer pump. The cold side outlet of the steam heater D is connected to the inlet of the desoaping centrifuge. The light phase desoaping oil outlet of the desoaping centrifuge is connected to the upper inlet of the water washing buffer section. The bottom outlet of the water washing buffer section is connected to the inlet of the water washing centrifuge. The light phase water washing oil outlet of the water washing centrifuge is connected to the water washing oil output pipe.

[0018] Further, the degumming section is a water degumming section, the water degumming section comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a water reaction section, a degumming vacuum drying section, a hot water tank and a soft water tank, the outlet of the raw oil pump is connected with the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected with the main inlet of the static water mixer, the water inlet of the static water mixer is connected with the outlet of the process hot water pipe, the outlet of the static water mixer is connected with the upper end inlet of the water reaction section in the integrated combined degumming tower, the lower end outlet of the water reaction section is connected with the inlet of the degumming centrifuge through the watered oil conveying pump, the light phase outlet of the degumming centrifuge is connected with the upper end inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected with the degumming vacuum pipe, the bottom outlet of the degumming vacuum drying section is connected with the degumming oil output pipe through the degumming dry oil conveying pump; the outlet of the hot water tank is connected with the inlet of the process hot water pipe through the hot water pump.

[0019] Further, the degumming section is an acid degumming section, the acid degumming section comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a primary acidification reaction section, a water reaction section and a degumming vacuum drying section, the outlet of the raw oil pump is connected with the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected with the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected with the acid pipe; the outlet of the static acid mixer A is connected with the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected with the main inlet of the static water mixer through the primary acidification oil conveying pump, the water inlet of the static water mixer is connected with the outlet of the process hot water pipe, the outlet of the static water mixer is connected with the upper end inlet of the water reaction section in the integrated combined degumming tower, the lower end outlet of the water reaction section is connected with the inlet of the degumming centrifuge through the watered oil conveying pump, the light phase outlet of the degumming centrifuge is connected with the upper end inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected with the degumming vacuum pipe, the bottom outlet of the degumming vacuum drying section is connected with the degumming oil output pipe through the degumming dry oil conveying pump.

[0020] Further, the outlet of the primary acidification oil conveying pump is connected with the hot side inlet of the water cooler A, the hot side outlet of the water cooler A is connected with the main inlet of the static water mixer, the water inlet of the static water mixer is also connected with the lye pipe; the outlet of the watered oil conveying pump is connected with the cold side inlet of the steam heater B, the cold side outlet of the steam heater B is connected with the inlet of the degumming centrifuge.

[0021] Further, the degumming section is an enzymatic degumming section, the enzymatic degumming section comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a primary acidification reaction section, an enzyme reaction section and a vacuum drying section, the outlet of the raw oil pump is connected with the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected with the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected with the acid liquid pipe, the outlet of the static acid mixer A is connected with the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected with the hot side inlet of the water cooler A through the primary acidification oil conveying pump, the hot side outlet of the water cooler A is connected with the main inlet of the static alkali mixer A, the alkali liquid inlet of the static alkali mixer A is connected with the alkali liquid pipe, the outlet of the static alkali mixer A is connected with the outlet of the enzyme preparation pipe and the inlet of the enzyme mixer, the outlet of the enzyme mixer is connected with the upper end inlet of the enzyme reaction section, the lower end outlet of the enzyme reaction section is connected with the cold side inlet of the steam heater B through the enzyme reaction section oil outlet pump, the cold side outlet of the steam heater B is connected with the inlet of the degumming centrifuge, the light phase outlet of the degumming centrifuge is connected with the upper end inlet of the vacuum drying section, the exhaust port of the vacuum drying section is connected with the degumming vacuumizing pipe, and the bottom outlet of the vacuum drying section is connected with the degumming oil output pipe through the degumming drying oil conveying pump.

[0022] Further, the hot water tank is further provided with a soft water tank below, the outlet of the soft water tank is connected with the inlet of the soft water pump, and the outlet of the soft water pump is connected with the water supplement port of the hot water tank and the flushing port of the degumming centrifuge through the soft water pipeline.

[0023] Further, the alkali refining section is provided with a decoloring section downstream, the decoloring section comprises an integrated combined decoloring tower, the integrated combined decoloring tower is sequentially stacked from top to bottom with a pulse dust collector, a decoloring agent temporary storage tank and a decoloring reaction section, the decoloring reaction section comprises a static mixing structure located at the upper side and a stirring decoloring section located at the lower side;

[0024] The inlet of the decoloring agent temporary storage tank is connected with the outlet of the decoloring agent conveying pipe, the top outlet of the decoloring agent temporary storage tank is connected with the inlet of the pulse dust collector, and the top outlet of the pulse dust collector is connected with the atmosphere through the dust removal fan;

[0025] The bottom outlet of the decoloring agent temporary storage tank is connected with the decoloring agent inlet of the static mixing structure through a metering addition rotary valve, the outlet of the alkali refining oil output pipe is connected with the cold side inlet of the steam heater E, the cold side outlet of the steam heater E is connected with the oil liquid inlet of the static mixing structure, the bottom outlet of the stirring decoloring section is connected with the oil inlet of the decoloring filter through the filter feeding pump, and the intermediate oil outlet of the decoloring filter is connected with the decoloring oil output pipe.

[0026] Further, the integrated combined bleaching tower is provided with an intermediate oil tank at the bottom, and the bleaching filters are provided in parallel with at least two, and the oil inlet and the intermediate oil outlet of each bleaching filter are connected with the waste oil collecting pipe through valves respectively, the outlet of the waste oil collecting pipe is connected with the upper inlet of the intermediate oil tank, and the bottom outlet of the intermediate oil tank is connected with the upper oil return port of the stirring bleaching section through a siphon oil return pipe.

[0027] Further, the stirring bleaching section is a steam stirring bleaching section or a jet stirring bleaching section.

[0028] Further, the upper sidewall air outlet of the stirring bleaching section is connected with the inlet of the gas-liquid separator, the top outlet of the gas-liquid separator is connected with the bleaching vacuum pipe, and the bottom outlet of the gas-liquid separator is connected with the upper oil return port of the stirring bleaching section.

[0029] Further, the upper outlet of the shell of each bleaching filter is connected with the top flow oil return pipe through a valve respectively, the outlet of the top flow oil return pipe is connected with the upper inlet of the intermediate oil tank, and the top exhaust port of the intermediate oil tank is connected with the bleaching vacuum pipe.

[0030] Further, a deodorization section is arranged downstream of the bleaching section, the deodorization section comprises an integrated combined deodorization tower, the integrated combined deodorization tower is sequentially stacked from top to bottom with a fatty acid trap, a post-deacidification tower section, a pre-deacidification tower section and a plate tower stripping section, the bleaching oil output pipe is connected with the upper inlet of the gas release chamber, the bottom outlet of the gas release chamber is connected with the lower inlet of the shell side of the falling film economizer through a gas release oil delivery pump, the upper outlet of the shell side of the falling film economizer is connected with the oil inlet of the pre-deacidification tower section, the bottom of the pre-deacidification tower section is connected with the upper part of the plate tower stripping section, the bottom oil outlet of the plate tower stripping section is connected with the cold side inlet of the falling film heater through a plate tower oil delivery pump, the cold side outlet of the falling film heater is connected with the upper oil inlet of the post-deacidification tower section, the lower oil outlet of the post-deacidification tower section is connected with the hot side inlet of the falling film economizer, the hot side outlet of the falling film economizer is connected with the inlet of the deodorization oil delivery pump; the top gas phase port of the post-deacidification tower section is connected with the bottom of the fatty acid trap, and the top exhaust port of the fatty acid trap is connected with the deodorization vacuum pipe.

[0031] Further, the bottom liquid outlet of the fatty acid trap is connected with the inlet of the fatty acid circulating pump, the outlet of the fatty acid circulating pump is connected with the fatty acid discharge pipe and the hot side inlet of the water cooler B respectively, and the hot side outlet of the water cooler B is connected with the top spray port of the fatty acid trap.

[0032] Further, the falling film economizer is arranged in the center suction cylinder of the plate tower stripping section, and the annular space between the center suction cylinder and the plate tower stripping section cylinder is provided with multiple layers of trays, and each layer of tray is provided with a stripping pump; the circumference of the center suction cylinder is uniformly provided with air holes to communicate the gas phase space of the tray with the inner cavity of the center suction cylinder.

[0033] The inner cavity of the shell of the falling film economizer is provided with falling film tubes, the falling film tubes are arranged between the upper tube plate and the lower tube plate, and the upper portion of the upper tube plate is provided with an oil distribution plate; the lower end of the shell of the falling film economizer penetrates through the lower head of the plate tower stripping section, and the lower tube plate is connected with a deodorized oil buffer tank below, and the bottom of the deodorized oil buffer tank is provided with a deodorized oil outlet.

[0034] Further, each tray is provided with a partitioned inner cylinder coaxial with the plate tower stripping section cylinder, the inner side of the partitioned inner cylinder is an inner annular flow channel, and the outer side of the partitioned inner cylinder is an outer annular flow channel; a radial partition plate is arranged between the outer wall of the center suction cylinder and the inner wall of the plate tower stripping section cylinder; the outlet of the overflow pipe of the upper tray is bent towards the head end of the inner annular flow channel close to the radial partition plate, and the tail end of the partitioned inner cylinder close to the other side of the radial partition plate is provided with a notch connected with the head end of the outer annular flow channel.

[0035] Further, the tail end of the outer annular flow channel is provided with a tray overflow pipe overflowing to the head end of the next layer of inner annular flow channels, or the head end of the inner annular flow channel is provided with a tray overflow pipe overflowing to the tail end of the next layer of outer annular flow channels, or the tail end of the outer annular flow channel is provided with a tray overflow pipe overflowing to the tail end of the next layer of outer annular flow channels, and the head end of the inner annular flow channel is provided with a tray overflow pipe overflowing to the head end of the next layer of inner annular flow channels.

[0036] Further, each tray is arranged in an outer high and inner low inclined manner, and the lowest part of the tray is connected with a tray emptying pipe, the tray emptying pipe of each layer extends to the outside of the plate tower stripping section cylinder and is connected with the tray backflow port of the lower layer through an emptying valve, and the tray backflow port is located below the liquid surface of the outer annular flow channel.

[0037] Further, the lower portion of the center suction cylinder is provided with a suction cylinder reduced diameter section, the upper end of the suction cylinder reduced diameter section is located below the air hole of the bottom layer, the lower end of the suction cylinder reduced diameter section is provided with a liquid seal plate, and the liquid seal plate is provided with a liquid discharge small hole.

[0038] Further, the inner end of the oil inlet pipe of the falling film economizer is provided below with an oil dispersion cylinder uniformly overflowing to the oil distribution plate, the oil distribution plate is fixed above the upper tube plate of the falling film economizer through support bolts, the oil distribution plate is uniformly provided with multiple oil distribution holes which are narrow at the top and wide at the bottom, the projections of the oil distribution holes are symmetrically distributed around the upper tube port of each falling film tube in a regular triangle shape; and the oil distribution plate is uniformly provided with gas permeation tubes penetrating through the oil layer.

[0039] Compared with the prior art, the present invention has achieved the following beneficial effects: 1. The integrated combined degumming tower replaces the traditional non-standard container equipment such as hydration tank, acidification tank, enzyme reaction tank, vacuum drying tower, soft water tank, and hot water tank, which simplifies the process design of the hydration degumming section, reduces equipment manufacturing costs, saves installation materials, and reduces building area, thereby effectively reducing project construction costs and shortening the project construction cycle.

[0040] 2. The integrated degumming tower uses a jet stirring device inside the hydration reaction section, acidification reaction section and enzyme reaction section, which is combined with an external oil circulation pump to replace the traditional paddle mechanical stirring. This improves reaction efficiency, product quality and equipment operation reliability, reduces the consumption of acid and alkali auxiliary materials and oil loss, shortens system start-up and shutdown time and reduces system inventory.

[0041] 3. The degumming process uses static water mixers, static acid mixers, and static alkali mixers instead of traditional power mixers, which are easy to install directly in the pipeline and reduce energy consumption.

[0042] 4. The integrated combined alkali refining tower replaces the traditional non-standard container equipment such as acidification tanks, alkali reaction tanks, and water washing buffer tanks, which simplifies the process design of the alkali refining section, reduces equipment manufacturing costs, saves installation materials, and reduces building area, thereby effectively reducing project construction costs and shortening the project construction cycle.

[0043] 5. The secondary acidification reaction section, alkali reaction section and water washing buffer section of the combined alkali refining tower adopt a jet stirring device, which is combined with an external oil circulation pump to replace the traditional paddle mechanical stirring. This improves reaction efficiency, product quality and equipment operation reliability, and reduces the consumption of auxiliary materials such as acid, alkali, and washing water, as well as grease loss. At the same time, it improves equipment operation reliability, shortens system start-up and shutdown time, and reduces system inventory.

[0044] 6. The integrated combination decolorization tower replaces the traditional non-standard container equipment such as decolorizing agent storage tanks, premixing tanks, decolorization towers, and sludge tanks, which simplifies the process design of the decolorization section, reduces equipment manufacturing costs, saves installation materials, and reduces building area, thereby effectively reducing project construction costs and shortening the project construction cycle.

[0045] 7. The metering rotary valve of the integrated combined decolorization tower adopts a continuous metering method instead of the traditional AB valve and metering cylinder. The decolorization reaction section adopts a static mixing structure instead of the traditional mechanical stirring and mixing, which improves the mixing efficiency of decolorizing agent and oil, reduces the consumption of decolorizing agent auxiliary materials, improves product quality and equipment operation reliability, reduces oil loss, reduces system inventory, and shortens system start-up and shutdown time.

[0046] 8. The integrated combined deodorization tower replaces traditional fatty acid traps, pre-deacidification towers, post-deacidification towers, plate towers, gas separation chambers and other non-standard container equipment, simplifying the deodorization section process design, reducing equipment manufacturing costs, saving installation materials, reducing building area, thereby effectively reducing project construction costs and shortening project construction period;

[0047] 9. The falling film heat exchange structure replaces the traditional immersed tube heat exchange or coil heat exchange structure, improves the heat exchange efficiency, significantly reduces the residence time of oil at high temperature, and improves the nutritional quality of refined oil; at the same time, it significantly reduces the storage capacity in the system, shortens the system start-up and shutdown time;

[0048] 11. For a large-capacity deodorization section, the falling film energy saver for cold and hot oil heat exchange is placed in the center of the plate tower stripping section, further integrating the falling film energy saver without heat loss and the need for insulation, and the deodorized oil in the falling film tube is cooled under vacuum, with high heat exchange efficiency, short residence time, no mixing, and effectively avoiding the generation of trans-acid and harmful polymers.

[0049] 11. The plate tower stripping section of the integrated combined deodorization tower is in low temperature mode, taking into account the necessary residence time, and the generation of thermal decomposition, thermal decolorization, trans-acid and polymer is controlled, and each layer of the plate tower stripping section can adjust the residence time of oil in the plate tower stripping section according to process requirements.

[0050] 12. The integrated combined deodorization tower makes full use of the center cylinder space in the tower to integrate cold and hot oil heat exchange into the center gas phase exhaust cylinder of the plate tower stripping section, without heat loss and the need for insulation, with vacuum falling film cooling of finished oil in the tube, high heat exchange efficiency, short residence time, no mixing, and effectively avoiding the generation of trans-acid and harmful polymers; the cold oil after heat exchange directly meets the process requirements of low-temperature deodorization, saving oil heating devices.

[0051] 13. The integrated combined deodorization tower saves flange sealing at the upper oil distribution plate position of the built-in energy-saving heat exchanger, saves manufacturing materials, is easy to disassemble and assemble, and completely eliminates the oxidation of finished oil caused by air contact due to leakage.

[0052] 14. The integrated combined deodorization tower, the integrated combined alkali refining tower, the integrated combined decolorization tower and the integrated combined deodorization tower all adopt modular design, saving installation space and land area, reducing the amount of installation materials, reducing device costs, saving a large number of pipeline connections, fully utilizing oil gravity flow to save unnecessary pump transportation, reducing factory investment and subsequent production and maintenance costs; at the same time, it solves the problems of large fluid resistance, heat loss, leakage risk of corrugated pipes and valves, and can be flexibly configured according to the characteristics of oil and process index requirements. BRIEF DESCRIPTION OF DRAWINGS

[0053] In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings needed to be used in the embodiments will be briefly introduced as follows. Obviously, the drawings in the following description are only some embodiments of the present application, and for those skilled in the art, other drawings can be obtained from these drawings without any creative effort, and the drawings are provided for reference and illustration only, not to limit the present application. Among them:

[0054] Figure 1 The flow chart of the water degumming section in the present application;

[0055] Figure 2 The flow chart of the acid degumming section in the present application;

[0056] Figure 3 The flow chart of the super degumming section in the present application;

[0057] Figure 4 The flow chart of the enzymatic degumming section in the present application;

[0058] Figure 5 The flow chart of the alkali refining section in the present application;

[0059] Figure 6 The flow chart of the decolorization section in the present application;

[0060] Figure 7 The flow chart of the decolorization section in the present application;

[0061] Figure 8 The flow chart of the deodorization section in the present application;

[0062] Figure 9 The flow chart of the deodorization section in the present application;

[0063] Figure 10 The cross-sectional view of an embodiment of the stripping section in the present application; Figure 9 The cross-sectional view of an embodiment of the stripping section in the present application;

[0064] The cross-sectional view of an embodiment of the stripping section in the present application; Figure 11 The cross-sectional view of an embodiment of the stripping section in the present application; Figure 10 The cross-sectional view of an embodiment of the stripping section in the present application; The cross-sectional view of an embodiment of the stripping section in the present application;

[0065] The cross-sectional view of an embodiment of the stripping section in the present application; Figure 12 The cross-sectional view of an embodiment of the stripping section in the present application; Figure 10 The cross-sectional view of an embodiment of the stripping section in the present application; The cross-sectional view of an embodiment of the stripping section in the present application;

[0066] The cross-sectional view of an embodiment of the stripping section in the present application; Figure 13 The cross-sectional view of an embodiment of the stripping section in the present application;

[0067] In the figure: 1. Steam heater A; 2. Static acid mixer A; 2a. Static water mixer;

[0068] 3. Integrated degumming tower; 3a. Primary acidification reaction section; 3b. Enzyme reaction section; 3c. Degumming vacuum drying section; 3d. Hot water tank; 3e. Soft water tank; 3f. Hydration reaction section;

[0069] 4. Static alkali mixer A; 5. Degumming centrifuge; 6. Steam heater B; 7. Water cooler A; 8. Enzyme mixer; 9. Steam heater C; 10. Static acid mixer B;

[0070] 11. Integrated alkali refining tower; 11a. Secondary acidification reaction section; 11b. Alkali reaction section; 11c. Water washing buffer section; 11d. Alkali refining vacuum drying section;

[0071] 12. Static alkali mixer B; 13. Steam heater D; 14. Soap removal centrifuge; 15. Water washing centrifuge; 16. Steam heater E;

[0072] 17. Integrated bleaching tower; 17a. Pulse dust collector; 17b. Bleaching agent temporary storage tank; 17c. Metering addition rotary valve; 17d. Bleaching reaction section; 17e. Middle oil tank;

[0073] 18. Bleaching filter; 19. Dust removal fan; 20. Gas-liquid separator;

[0074] 21. Integrated deodorization tower; 21a. Fatty acid catcher; 21b. Post-deacidification tower section; 21c. Pre-deacidification tower section;

[0075] 21d. Tray tower stripping section; 21d1. Subsection inner cylinder; 21d2. Radial partition; 21d3. Tray overflow pipe; 21d4. Stripping pump; 21d5. Tray tower stripping section annular jet pipe;

[0076] 21e. Gas separation chamber; 21e1. Bleaching oil inlet; 21e2. Bleaching oil spray pipe; 21e3. Pre-degassing vacuum extraction port; 21e4. Gas separation chamber oil outlet;

[0077] 22. Falling film economizer; 22a. Oil dispersion cylinder; 22b. Oil distribution plate; 22c. Air permeable pipe; 22d. Support bolt; 22e. Upper tube sheet; 22f. Falling film tube bundle; 22g. Lower shell side inlet; 22h. Upper shell side outlet; 22j. Deodorized oil buffer tank; 22k. Deodorized oil outlet;

[0078] 23. Falling film heater; 24. Water cooler B;

[0079] P1. raw oil pump; P2. primary acidification oil delivery pump; P2a. hydrated oil delivery pump; P3. primary acidification oil circulating pump; P3a. hydrated oil circulating pump; P4. enzyme reaction section oil delivery pump; P5. enzyme reaction section circulating pump; P6. degummed dry oil delivery pump; P7. hot water pump; P8. soft water pump; P9. secondary acidification oil delivery pump; P10. secondary acidification oil circulating pump; P11. neutralized oil delivery pump; P12. neutralized oil circulating pump; P13. water washed oil circulating pump; P14. caustic refining dry oil delivery pump; P15. filter feed pump; P16. bleached oil circulating pump; P17. gassed oil delivery pump; P18. plate and tower oil delivery pump; P19. deodorized oil delivery pump; P20. fatty acid circulating pump;

[0080] G1. raw oil line; G2. acid liquid pipe; G3. degummed oil output pipe; G4. steam pipe; G5. degumming vacuum pipe; G6. process hot water pipe; G7a. soft water supply pipe; G7b. soft water supply pipe; G8. lye pipe; G9. enzyme preparation pipe; G10. caustic refining vacuum pipe; G11. caustic refining oil output pipe; G12. bleaching agent delivery pipe; G13. filter feed pipe; G14. bleaching vacuum pipe; G15. top flow oil return pipe; G16. intermediate circulating pipe; G17. dirty oil collection pipe; G18. siphon oil return pipe; G19. bleached oil output pipe; G20. deodorized oil output pipe; G21. fatty acid discharge pipe; G22. deodorizing vacuum pipe. DETAILED DESCRIPTION

[0081] In the following description of the present application, the terms "upper", "lower", "front", "back", "left", "right", "inner", "outer" and the like indicate the orientation or positional relationship based on the orientation or positional relationship shown in the drawings, only for the convenience of describing the present application and simplifying the description, and do not mean that the device must have a particular orientation. The percentages not specified herein are all weight percentages.

[0082] In order to make the technical means, creative features, purposes and effects of the present application easy to understand, the present application is further described below in combination with specific drawings. Obviously, the described embodiments are only a part of the embodiments of the present application, not all.

[0083] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used in the description of the application herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the application.

[0084] The integrated plant oil refining system of the present application comprises, in sequence, a degumming section, a caustic refining section, a bleaching section and a deodorizing section.

[0085] As Figure 1As shown, one of the degumming sections in the present application is a hydration degumming section. The principle of hydration degumming is to use the hydrophilic property of phospholipids to make the hydrated phospholipids swell and coagulate by absorbing water, and then separate them from the oil by centrifugation. At the same time, it can adsorb proteins, mucilage and trace metal ions combined with phospholipids. Hydration degumming can only remove hydrated phospholipids, but it is difficult to remove non-hydrated phospholipids. The oil after hydration degumming generally contains 100-200 ppm of phosphorus. At present, most edible oil processing plants use hydration degumming technology to separate phospholipids from oil, further separate and purify them, and make high-value health care products to improve the economic efficiency of enterprises.

[0086] The hydration degumming section includes a steam heater 1, a static water mixer 2a, an integrated combined degumming tower 3, and a degumming centrifuge 5. The integrated combined degumming tower 3 includes a hydration reaction section 3f, a degumming vacuum drying section 3c, a hot water tank 3d, and a soft water tank 3e stacked in order from top to bottom.

[0087] The outlet of the raw material pipeline G1 is connected to the inlet of the raw oil pump P1. The outlet of the raw oil pump P1 is connected to the cold side inlet of the steam heater 1. The hot side inlet of the steam heater 1 is connected to the steam pipe G4. The cold side outlet of the steam heater 1 is connected to the main inlet of the static water mixer 2a. The water inlet of the static water mixer 2a is connected to the process hot water pipe G6. The outlet of the static mixer 2 is connected to the top inlet of the hydration reaction section 3f at the top of the integrated combined degumming tower 3. The outlet of the hydration reaction section 3f is connected to the inlet of the hydration oil delivery pump P2a. The outlet of the hydration oil delivery pump P2a is connected to the inlet of the degumming centrifuge 5. The light phase outlet of the degumming centrifuge 5 is connected to the upper inlet of the degumming vacuum drying section 3c in the integrated combined degumming tower 3. The top exhaust port of the degumming vacuum drying section 3c is connected to the degumming vacuum pumping pipe G5. The lower outlet of the degumming vacuum drying section 3c is connected to the inlet of the degumming dry oil delivery pump P6. The outlet of the degumming dry oil delivery pump P6 is connected to the degumming oil output pipe G3. At the same time, the hot water tank 3d and the soft water tank 3e are arranged in the lower section of the integrated combined degumming tower 3 to supply hot process water and soft water for the degumming section.

[0088] The raw oil from the raw material pipeline G1 is delivered into the cold side of the steam heater A1 by the raw oil pump P1, exchanges heat with the steam in the hot side, and the oil temperature is raised from 30 DEG C to 80 DEG C-85 DEG C, and then enters the static water mixer 2a to be mixed with a certain proportion of 85 DEG C-90 DEG C process hot water, the process hot water is added in a proportion of 1-3% of the oil weight, and after mixing, enters the hydration reaction section 3f of the integrated combined degumming tower 3 to carry out hydration reaction, and the hydration reaction time is about 30 minutes; in the hydration reaction section, the hydrophilic gum in the raw oil is combined with water and coagulates into macromolecular colloidal particles. The reacted hydration oil is delivered by the hydration oil delivery pump P2a, enters the degumming centrifuge 5, the water content of the separated light phase degumming oil is about 0.5%, enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 to carry out drying and dehydration, the water content of the dried oil after dehydration is about 0.05%, and the degumming dried oil is delivered by the degumming dried oil delivery pump P6 and the degumming oil output pipe G3 to the degumming section.

[0089] The hydration reaction section 3f of the integrated combined degumming tower 3 is internally provided with a plurality of stages of jet mixers, the hydration oil discharged from the bottom of the hydration reaction section 3f is delivered by the hydration oil circulating pump P3a, enters the stages of jet mixers, and realizes full mixing reaction of the hydration oil.

[0090] In the integrated combined degumming tower 3, the water supplement pipe G7a is connected with the water supplement pipe G7a, the bottom outlet of the soft water tank 3e is connected with the inlet of the soft water pump P8, the outlet of the soft water pump P8 is connected with the water supplement pipe G7b of the hot water tank 3d through the soft water supply pipe G7b, and is used for preparation of process hot water and hydration degumming reaction of raw oil. The soft water supply pipe G7b is also connected with the clean water inlet of the degumming centrifuge 5, and is used for drum flushing operation of the degumming centrifuge 5.

[0091] The bottom outlet of the hot water tank 3d is connected with the inlet of the hot water pump P7, and the outlet of the hot water pump P7 is connected with the process hot water pipe G6. After the softened water is injected into the hot water tank 3d, the softened water is heated to hot water by steam, and the hot water is sent to the water inlet of the static water mixer 2a and the inlet pipeline of the degumming centrifuge 5 by the hot water pump P7 through the process hot water pipe G6.

[0092] As shown in Figure 2 The second degumming section in the application is an acidification degumming section, and the acid degumming is to further remove phospholipids in the oil. Generally, some organic acid such as citric acid or inorganic acid such as phosphoric acid is added into the raw oil to convert the non-hydrated phospholipids in the oil into hydrated phospholipids which are easy to remove, neutralize the surface charge points of the colloidal dispersed phase particles to make them aggregate and settle, and also make the metal ions such as calcium, magnesium and iron which are combined with the phospholipids into free state and transfer to the water phase, so as to achieve the effect of removing impurities. The acid degumming technology is the most effective and most commonly used method for removing non-hydrated phospholipids in oil.

[0093] The acid degumming section comprises a steam heater A1, a static acid mixer A2, an integrated combined degumming tower 3, a static water mixer 2a and a degumming centrifuge 5. The integrated combined degumming tower 3 comprises, from top to bottom, a primary acidification reaction section 3a, a hydration reaction section 3f, a degumming vacuum drying section 3c, a hot water tank 3d and a soft water tank 3e.

[0094] The raw material pipeline G1 is connected to the inlet of a raw oil pump P1. The outlet of the raw oil pump P1 is connected to the cold side inlet of the steam heater A1. The hot side inlet of the steam heater A1 is connected to the steam pipeline G4. The cold side outlet of the steam heater A1 is connected to the main inlet of the static acid mixer A2. The acid inlet of the static acid mixer A2 is connected to the acid pipeline G2. The outlet of the static acid mixer A2 is connected to the top inlet of the primary acidification reaction section 3a at the top of the integrated combined degumming tower 3. The bottom outlet of the primary acidification reaction section 3a is connected to the inlet of a primary acidification oil delivery pump P2. The outlet of the primary acidification oil delivery pump P2 is connected to the main inlet of the static water mixer 2a. The water inlet of the static water mixer 2a is connected to the process hot water pipeline G6. The outlet of the static water mixer 2a is connected to the top inlet of the hydration reaction section 3f in the integrated combined degumming tower 3. The outlet of the hydration reaction section 3f is connected to the inlet of a hydration oil delivery pump P2a. The outlet of the hydration oil delivery pump P2a is connected to the inlet of the degumming centrifuge 5. The light phase outlet of the degumming centrifuge 5 is connected to the upper inlet of the degumming vacuum drying section 3c in the integrated combined degumming tower 3. The top exhaust port of the degumming vacuum drying section 3c is connected to the degumming vacuum pumping pipeline G5. The lower outlet of the degumming vacuum drying section 3c is connected to the inlet of a degumming dry oil delivery pump P6. The outlet of the degumming dry oil delivery pump P6 is connected to the degumming oil output pipeline G3. Meanwhile, the hot water tank 3d and the soft water tank 3e are arranged at the lower section of the integrated combined degumming tower 3 for supplying hot process water and soft water for the degumming section.

[0095] The raw oil from the raw material pipeline G1 is delivered into the cold side of the steam heater A1 by the raw oil pump P1, exchanges heat with the steam in the hot side, and the oil temperature is raised from 30℃ to 80-85℃, and then enters the static acid mixer B1 to mix with a certain proportion of acid, usually the addition ratio of acid is about 0.05-0.2% of the oil weight; then enters the integrated combined degumming tower 3 for acidification reaction in the first acidification reaction section 3a, and the acidification reaction time is about 60 minutes; part of the non-hydrated phospholipids in the oil is converted into hydrated phospholipids, and the acidified oil after reaction is sent out by the first acidified oil delivery pump P2, and then enters the static water mixer 2a to mix with a certain proportion of 85-90℃ process hot water, and the addition ratio of process hot water is about 1-3% of the oil weight; then enters the hydration reaction section 3f of the integrated combined degumming tower 3 for hydration reaction, and the hydration reaction time is about 30 minutes; the hydrated oil after reaction is sent out by the hydrated oil delivery pump P2a, enters the degumming centrifuge 5, and the hydrated phospholipids combine with the process hot water to form a colloid and separate from the oil, thereby reducing the phospholipid content in the oil and improving the frying quality of the oil. The light phase degummed oil separated from the degumming centrifuge 5 has a water content of about 0.5%, enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 for drying and dehydration, and the dried oil after dehydration has a water content of about 0.05%, which is delivered out of the degumming section by the degumming dried oil delivery pump P6 and the degummed oil output pipe G3.

[0096] The integrated combined degumming tower 3 is provided with a plurality of stages of jet mixers inside the first acidification reaction section 3a, the acidified oil in the first acidification reaction section 3a is delivered by the first acidification oil circulating pump P3, enters each stage of jet mixers, and realizes sufficient mixing reaction of the acidified oil.

[0097] The hydration reaction section 3f is provided with a plurality of stages of jet mixers inside, the hydrated oil discharged from the bottom of the hydration reaction section 3f is sent out by the hydrated oil circulating pump P3a, enters each stage of jet mixers, and realizes sufficient mixing reaction of the hydrated oil.

[0098] In the integrated combined degumming tower 3, the water supplement pipe G7a is connected to the water supplement port of the soft water tank 3e, the bottom outlet of the soft water tank 3e is connected to the inlet of the soft water pump P8, the outlet of the soft water pump P8 is connected to the water supplement port of the hot water tank 3d and the clean water inlet of the degumming centrifuge 5 through the soft water supply pipe G7b, and is used for supplying cold process water in the degumming section.

[0099] The bottom outlet of the hot water tank 3d is connected to the inlet of the hot water pump P7, and the outlet of the hot water pump P7 is connected to the process hot water pipe G6. After the softened water is injected into the hot water tank 3d, it is heated to hot water by steam, and the hot water is sent to the water inlet of the static water mixer 2a and the inlet pipeline of the degumming centrifuge 5 by the hot water pump P7 through the process hot water pipe G6.

[0100] As Figure 3As shown, the third degumming section in the present application is a super degumming section. The super degumming is to remove the phospholipid in the oil completely. Some organic acid such as citric acid or inorganic acid such as phosphoric acid is added to the raw oil to convert the non-hydrated phospholipid in the oil into hydrated phospholipid which is easy to remove. The surface charge point of the colloidal dispersed phase particles is neutralized to make them aggregate and settle. At the same time, the metal ions such as calcium, magnesium and iron which are combined with the phospholipid are changed into free state and transferred to the water phase, thereby achieving the effect of removing impurities. After the raw oil is acidified and conditioned, a certain amount of alkali is added as a flocculating agent for water degumming, and the phospholipid is further removed. The super degumming technology is one of the important methods for completely removing the heavy phospholipid and other gums in the oil. The oil after super degumming generally contains 5-20 ppm of phosphorus.

[0101] The unmarked part is the same as the acid degumming section, and a static water mixer 2a, a steam heater B 6 and a water cooler A 7 are added.

[0102] The outlet of the primary acid oil delivery pump P2 is connected to the hot side inlet of the water cooler A 7, the cold side inlet of the water cooler A 7 is connected to a cooling water pipe, the hot side outlet of the water cooler A 7 is connected to the main inlet of the static water mixer 2a, and the water inlet of the static water mixer 2a is connected to the process hot water pipe G6 and the lye pipe G8.

[0103] The outlet of the hydrated oil delivery pump P2a is connected to the cold side inlet of the steam heater B 6, the hot side of the steam heater B 6 is connected to the steam pipe G4, and the cold side outlet of the steam heater B 6 is connected to the inlet of the degumming centrifuge.

[0104] The raw oil from the raw material pipeline G1 is delivered into the cold side of the steam heater A1 by the raw oil pump P1, exchanges heat with the steam in the hot side, and the oil temperature is raised from 30°C to 80-85°C, and then is mixed with a certain proportion of acid in the static acid mixer A2, enters the acidification reaction section 3a of the integrated combined degumming tower 3 to carry out acidification reaction, and the acidification reaction time is about 60 minutes; part of the non-hydrated phospholipid in the oil is converted into hydrated phospholipid, and the acidified oil after reaction is sent out by the primary acidified oil delivery pump P2, enters the hot side of the water cooler A7, exchanges heat with the circulating cooling water in the cold side, and the oil temperature is reduced from 80°C to 40°C, which is beneficial to the hydration and condensation of phospholipid; after cooling, it enters the static water mixer 2a, mixes with a certain proportion of process hot water at 85-90°C, and a small amount of lye is added, the addition proportion of lye is about 1-3% of the oil weight, the lye concentration is 1-2%, and the lye temperature is 85-90°C; after mixing, it enters the hydration reaction section 3f of the integrated combined degumming tower 3 to carry out hydration reaction, and the reaction time is about 60 minutes; the hydrated oil after reaction is sent out by the hydrated oil delivery pump P2a, enters the cold side of the steam heater B6, exchanges heat with the steam in the hot side, and the oil temperature is raised from 40°C to 80°C, which is beneficial to the separation of oil and colloid; then it enters the degumming centrifuge 5, the hydrated phospholipid combines with the process hot water to form colloid and is separated from the oil, thereby reducing the phospholipid content in the oil and improving the frying quality of the oil. The light phase degummed oil separated from the degumming centrifuge 5 contains about 0.5% of water, enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 to carry out drying and dehydration, and the dried oil after dehydration contains about 0.05% of water, which is delivered out of the degumming section by the degumming dried oil delivery pump P6 and the degummed oil output pipe G3.

[0105] As shown in Figure 4 The fourth degumming section in the present application is an enzymatic degumming section. Enzymatic degumming is a new type of degumming process. Commonly used enzymes include phospholipase PLA1, PLA2 and PLC. Among them, phospholipase PLA1 and phospholipase PLA2 can specifically hydrolyze the ester bond of phospholipid glycerol Sn-1 or Sn-2 to generate hydrophilic lysophospholipid and free fatty acid, thereby achieving the purpose of dephosphorization. PLC mainly acts on the glycerophosphate bond at C3 of glycerophospholipid, and the hydrolysis product is diglyceride (DAG) and organic phosphate (phosphocholine, phosphoethanolamine, phosphoserine and phosphoinositol, etc.), thereby achieving the purpose of dephosphorization. The enzymatic degumming process has the advantages of mild operating conditions, complete dephosphorization (degummed oil containing ≤10 ppm of phosphorus), less wastewater discharge and high yield of refined oil.

[0106] The enzymatic degumming section includes a steam heater A1, a static acid mixer A2, an integrated combined degumming tower 3, a static alkali mixer A4 and a degumming centrifuge 5. The integrated combined degumming tower 3 includes, from top to bottom, an acidification reaction section 3a, an enzyme reaction section 3b, a degumming vacuum drying section 3c, a hot water tank 3d and a soft water tank 3e.

[0107] The outlet of the raw material pipeline G1 is connected with the inlet of the raw oil pump P1, the outlet of the raw oil pump P1 is connected with the cold side inlet of the steam heater A1, the hot side inlet of the steam heater A1 is connected with the steam pipeline G4, the cold side outlet of the steam heater A1 is connected with the main inlet of the static acid mixer A2, the acid liquid inlet of the static acid mixer A2 is connected with the acid liquid pipeline G2; the outlet of the static acid mixer A2 is connected with the top inlet of the primary acidification reaction section 3a at the top of the integrated combined degumming tower 3, the bottom outlet of the primary acidification reaction section 3a is connected with the inlet of the primary acidification oil conveying pump P2, the outlet of the primary acidification oil conveying pump P2 is connected with the hot side inlet of the water cooler A7, the cold side inlet of the water cooler A7 is connected with the cooling water pipeline, the hot side outlet of the water cooler A7 is connected with the main inlet of the static alkali mixer A4, the alkali liquid inlet of the static alkali mixer A4 is connected with the alkali liquid pipeline G8, the outlet of the static alkali mixer A4 is connected with the inlet of the enzyme mixer 8, the inlet of the enzyme mixer 8 is also connected with the enzyme preparation pipeline G9, and the enzyme preparation is added into the oil liquid. The outlet of the enzyme mixer 8 is connected with the top inlet of the enzyme reaction section 3b in the integrated combined degumming tower 3, the outlet of the enzyme reaction section 3b is connected with the inlet of the enzyme reaction section oil outlet pump P4, the outlet of the enzyme reaction section oil outlet pump P4 is connected with the cold side inlet of the steam heater B6, the hot side of the steam heater B6 is connected with the steam pipeline G4, the cold side outlet of the steam heater B6 is connected with the inlet of the degumming centrifuge 5, the light phase outlet of the degumming centrifuge 5 is connected with the upper inlet of the degumming vacuum drying section 3c in the integrated combined degumming tower 3, the top exhaust port of the degumming vacuum drying section 3c is connected with the degumming vacuum pumping pipeline G5, the lower outlet of the degumming vacuum drying section 3c is connected with the inlet of the degumming dry oil conveying pump P6, and the outlet of the degumming dry oil conveying pump P6 is connected with the degumming oil output pipeline G3. Meanwhile, the hot water tank 3d and the soft water tank 3e are arranged at the lower section of the integrated combined degumming tower 3, and are used for supplying the hot process water and the soft water in the degumming section.

[0108] The raw oil from the raw oil pipeline G1 is delivered into the cold side of the steam heater A1 by the raw oil pump P1, and exchanges heat with the steam in the hot side, so that the oil temperature is raised from 30°C to 80-85°C, and then enters the static acid mixer A2 to be mixed with a certain proportion of acid, and the proportion of the acid is usually 0.05-0.2% of the oil weight; then enters the primary acidification reaction section 3a of the integrated combined degumming tower 3 to perform acidification reaction, so that part of the non-hydrated phospholipids in the oil is converted into hydrated phospholipids, and the reaction time is 60 minutes; the acidified oil after the reaction is sent out by the primary acidified oil delivery pump P2, enters the hot side of the water cooler A7 to exchange heat with the circulating cooling water in the cold side, so that the oil temperature is reduced from 80°C to 55-60°C, which is beneficial to the hydration and condensation of the phospholipids; after the temperature is reduced, the oil enters the static alkali mixer A4 to be mixed with a certain proportion of alkali liquor, and the proportion of the alkali liquor is about 1-3% of the oil weight, the concentration of the alkali liquor is 1-2%, and the temperature of the alkali liquor is 85-90°C; the pH value of the oil is adjusted to 5-6, so as to create the best process condition for the enzyme catalytic hydrolysis. Then the oil is mixed with the enzyme preparation sent out by the enzyme preparation pipeline G9 in the enzyme mixer 8, and the proportion of the enzyme preparation is 25-50 ppm; after the mixing, the oil enters the enzyme reaction section 3b of the integrated combined degumming tower 3 to perform enzyme reaction, so that the remaining non-hydrated phospholipids in the oil are completely converted into hydrated phospholipids; the degummed oil after the reaction is sent out by the enzyme reaction section oil pump P4, enters the cold side of the steam heater B6 to exchange heat with the steam in the hot side, so that the oil temperature is raised from 40°C to 80-85°C, which is beneficial to the separation of the oil and the colloid; then the oil enters the degumming centrifuge 5 to separate the colloid from the oil, so as to reduce the content of the phospholipids in the oil and improve the frying quality of the oil. The light phase degummed oil separated from the degumming centrifuge 5 has a water content of about 0.5%, enters the degumming vacuum drying section 3c of the integrated combined degumming tower 3 to perform drying and dehydration, and the dried oil after the dehydration has a water content of about 0.05%, which is delivered out of the degumming section by the degummed dried oil delivery pump P6 and the degummed oil output pipeline G3.

[0109] The integrated combined degumming tower 3 is provided with a plurality of stages of jet mixers in the primary acidification reaction section 3a, and the acidified oil in the primary acidification reaction section 3a is delivered by the primary acidification oil circulating pump P3, enters the stages of jet mixers to realize the full mixing reaction of the acidified oil.

[0110] The enzyme reaction section 3b is provided with a plurality of stages of jet mixers, and the degummed oil discharged from the bottom of the enzyme reaction section 3b is sent out by the enzyme reaction section circulating pump P5, enters the stages of jet mixers to realize the full mixing reaction.

[0111] In the integrated combined degumming tower 3, the water supply port of the soft water tank 3e is connected with the soft water supply pipeline G7a, the bottom outlet of the soft water tank 3e is connected with the inlet of the soft water pump P8, the outlet of the soft water pump P8 is connected with the water supply port of the hot water tank 3d and the clean water inlet of the degumming centrifuge 5 through the soft water supply pipeline G7b, and is used for supplying the cold process water in the degumming section.

[0112] The bottom outlet of the hot water tank 3d is connected with the inlet of the hot water pump P7, and the outlet of the hot water pump P7 is connected with the process hot water pipe G6. After the softened water is injected into the hot water tank 3d, the softened water is heated into hot water by steam, and the hot water is sent to the alkali liquid inlet of the static alkali mixer 4 and the inlet pipeline of the degumming centrifuge 5 by the process hot water pipe G6 through the hot water pump P7.

[0113] As shown in Figure 5 The alkali refining section in the present application includes a steam heater C 9, a static acid mixer B 10, an integrated combined alkali refining tower 11, a static alkali mixer B 12, a steam heater D 13, a soap removal centrifuge 14, and a water washing centrifuge 15. The integrated combined alkali refining tower 11 is sequentially stacked from top to bottom with a water washing buffer section 11c, a secondary acidification reaction section 11a, and an alkali reaction section 11b.

[0114] The process principle of alkali refining is to generate sodium soap in oil by neutralization reaction between caustic soda solution and free fatty acid in crude oil, and then to separate the soap from oil by centrifugal separation. The soap stock has strong adsorption capacity, which can adsorb protein, slime, pigment and even mechanical impurities in crude oil and remove them together. In the crude oil, a part of phospholipids will also be saponified by the alkali solution to form soap stock precipitate.

[0115] The outlet of the degummed oil output pipe G3 is connected with the cold side inlet of the steam heater C 9, the cold side outlet of the steam heater C 9 is connected with the inlet of the static acid mixer B 10, the acid liquid inlet of the static acid mixer B 10 is connected with the acid liquid pipe G2, the outlet of the static acid mixer B 10 is connected with the inlet of the secondary acidification reaction section 11a of the upper part of the integrated combined alkali refining tower 11, the outlet of the secondary acidification reaction section 11a is connected with the inlet of the secondary acidification oil delivery pump P9, the outlet of the secondary acidification oil delivery pump P9 is connected with the inlet of the static alkali mixer B 12, the alkali liquid inlet of the static alkali mixer B 12 is connected with the alkali liquid pipe G8, the outlet of the static alkali mixer B 12 is connected with the inlet of the alkali reaction section 11b of the middle upper part of the integrated combined alkali refining tower 11, the outlet of the alkali reaction section 11b is connected with the inlet of the neutralized oil delivery pump P11, the outlet of the neutralized oil delivery pump P11 is connected with the cold side inlet of the steam heater D 13, the cold side outlet of the steam heater D 13 is connected with the inlet of the soap removal centrifuge 14, the light phase soap removal oil outlet of the soap removal centrifuge 14 is connected with the inlet of the water washing buffer section 11c at the top of the alkali refining combined tower 3, the outlet of the water washing buffer section 11c is connected with the inlet of the water washing centrifuge 15, and the light phase water washing oil outlet of the water washing centrifuge 15 is connected with the water washing oil output pipe.

[0116] The integrated combined alkali refining tower 11 is provided with an alkali refining vacuum drying section 11d below the alkali reaction section 11b. The outlet of the water washing oil output pipe is connected to the inlet of the alkali refining vacuum drying section 11d. The top gas outlet of the alkali refining vacuum drying section 11d is connected to the alkali refining vacuum pumping pipe G10. The outlet of the alkali refining vacuum drying section 11d is connected to the inlet of the alkali refining dry oil conveying pump P14. The outlet of the alkali refining dry oil conveying pump P14 is connected to the alkali oil output pipe G11.

[0117] The degummed oil from the degumming oil output pipe G3 enters the cold side of the steam heater C 9 and exchanges heat with the steam on the hot side of the steam heater C 9, so that the oil temperature rises from 30°C to 80°C. Then the oil enters the static acid mixer B 10 and mixes with a certain proportion of acid. The addition ratio of the acid is usually 0.05-0.2% of the oil weight. Then the oil enters the secondary acidification reaction section 11a at the upper part of the integrated combined alkali refining tower 11 and performs acidification reaction for 30-60 minutes. The acidified oil after reaction is conveyed by the secondary acidification oil conveying pump P9, enters the static alkali mixer B 12 and mixes with a certain proportion of alkali liquor. The addition ratio of the alkali liquor is about 1-2% of the oil weight, and the concentration of the alkali liquor is 9-12%. The temperature of the alkali liquor is 85-90°C. Then the oil enters the alkali reaction section 11b at the middle-upper part of the integrated combined alkali refining tower 11 and performs alkali reaction. The neutralized oil after reaction is conveyed by the neutralized oil conveying pump P11, enters the cold side of the steam heater D 13 and exchanges heat with the steam on the hot side, so that the oil temperature rises from 80°C to 85°C. Then the oil enters the desoaping centrifuge 14. The light phase desoaping oil separated out enters the water washing buffer section 11c at the top of the integrated combined alkali refining tower 11 and performs water washing operation. The addition ratio of the water washing water is about 2-5% of the oil weight, and the temperature is 85-90°C. A small amount of acid liquid can also be added according to the situation. Then the oil enters the water washing centrifuge 15. The light phase water washing oil separated out contains about 0.5% of water, enters the alkali refining vacuum drying section 11d at the middle-lower part of the integrated combined alkali refining tower 11 and performs drying and dehydration. The dry oil after dehydration contains about 0.05% of water, which is conveyed out of the alkali refining section by the alkali refining dry oil conveying pump P14.

[0118] The secondary acidification reaction section 11a at the upper part of the integrated combined alkali refining tower 11 is provided with multiple stages of jet mixers. The acidified oil discharged from the bottom of the secondary acidification reaction section 11a is conveyed by the secondary acidification oil circulating pump P10, enters each stage of the jet mixers in the secondary acidification reaction section 11a, and realizes full mixing reaction of the oil.

[0119] The alkali reaction section 11b is provided with multiple stages of jet mixers. The hydrated oil discharged from the bottom of the alkali reaction section 11b is conveyed by the neutralized oil circulating pump P12, enters each stage of the jet mixers in the alkali reaction section 11b, and realizes full mixing reaction of the neutralized oil.

[0120] The water washing buffer section 11c is internally provided with multi-stage jet mixers, and the water washing oil of the water washing buffer section 11c is transported by a water washing oil circulating pump P13 into the multi-stage jet mixers in the water washing buffer section 11c to realize sufficient mixing reaction of the water washing oil.

[0121] As shown in Figure 6 The decoloring section in the application comprises a steam heater 16, an integrated combined decoloring tower 17, a decoloring filter 18, a dust removal fan 19 and a gas-liquid separator 20, the integrated combined decoloring tower 17 is sequentially stacked from top to bottom with a pulse dust collector 17a, a decoloring agent temporary storage tank 17b, a metering and adding rotary valve 17c, a decoloring reaction section 17d and an intermediate oil tank 17e, the upper part of the decoloring reaction section 17d is provided with a static mixing structure, and the lower part is provided with a steam stirring decoloring section or a jet stirring decoloring section.

[0122] The decoloring process principle is that certain materials such as activated carbon, bentonite and attapulgite have strong selective adsorption effect on pigments and other impurities, and the oil is treated by the materials to remove pigments, oxidation products, metal ions, residual soap, residual phosphorus, pesticide residues and polycyclic aromatic hydrocarbons, so as to achieve the purpose of purifying the oil.

[0123] The outlet of the decoloring agent delivery pipe G12 is connected with the inlet of the decoloring agent temporary storage tank 17b at the upper part of the integrated combined decoloring tower 17, the top outlet of the decoloring agent temporary storage tank 17b is connected with the pulse dust collector 17a, the top outlet of the pulse dust collector 17a is connected with the inlet of the dust removal fan 19, and the outlet of the dust removal fan 19 is connected with an atmospheric connection pipe.

[0124] The bottom outlet of the decoloring agent temporary storage tank 17b is connected with the inlet of the metering and adding rotary valve 17c, and the lower end outlet of the metering and adding rotary valve 17c is connected with the inlet of the decoloring reaction section 17d.

[0125] The outlet of the alkali refined oil output pipe G11 is connected with the cold side inlet of the steam heater 16, the cold side outlet of the steam heater 16 is connected with the inlet of the decoloring reaction section 17d of the integrated combined decoloring tower 17, the outlet of the decoloring reaction section 17d is connected with the inlet of the filter feeding pump P15, the outlet of the filter feeding pump P15 is connected with the inlet of the decoloring filter 18, and the outlet of the decoloring filter 18 is connected with a decoloring oil output pipe G19.

[0126] In addition, the vacuum outlet of the decoloring reaction section 17d is connected with the inlet of the gas-liquid separator 20, the top outlet of the gas-liquid separator 20 is connected with a decoloring vacuum pump G14, and the bottom outlet of the gas-liquid separator 20 is connected with the inlet of the oil return pipe of the decoloring reaction section 17d. In addition, the bottom of the integrated combined decoloring tower 17 is integrated with the intermediate oil tank 17e, which is used for collecting and recycling the dirty oil in the decoloring filter switching process.

[0127] The alkali refined oil from the alkali refined oil output pipe G11 enters the cold side of the steam heater G16 and exchanges heat with the steam in the hot side, and the oil temperature is raised from 90°C to 110°C, and then enters the decoloring reaction section 17d in the middle of the integrated combined decoloring tower 17. Under the action of vacuum suction, the raw oil and the decoloring agent are fully mixed in the static mixing structure at the top of the decoloring reaction section 17d, and the addition ratio of the decoloring agent is 0.5-1.5% of the oil weight. The static mixing structure at the top of the decoloring reaction section 17d is composed of multiple static baffles, which can ensure the full mixing of the oil and the decoloring agent. The mixture of the oil and the decoloring agent then enters the steam stirring decoloring section of the decoloring reaction section 17d for decoloring, and the injection pipe of the steam stirring decoloring section is connected with the steam pipe G4.

[0128] The decoloring oil is sent out by the filtering feed pump P15, enters one of the decoloring filters 18 through the filtering feed pipe G13, and is filtered. The filtered clean oil is transported into the next section through the decoloring oil output pipe G19. The two decoloring filters work alternately to realize continuous production.

[0129] As shown in Figure 7 , the steam stirring decoloring section of the decoloring reaction section 17d can be replaced by a jet stirring decoloring section. When the jet stirring decoloring section is used, part of the decoloring oil is transported into the multi-stage jet stirring device inside the decoloring reaction section 17d by the decoloring oil circulating pump P16 for circulating mixing and stirring, so as to ensure that the decoloring process is carried out in the best state.

[0130] The decoloring agent for decoloring operation comes from the decoloring agent delivery pipe G12 and is first temporarily stored in the decoloring agent temporary storage tank 17b of the integrated combined decoloring tower 17 under the action of negative pressure. After the dust-containing gas is purified and dedusted by the pulse dust collector 17a, the clean air is discharged to the atmosphere by the dust removal fan 19. The decoloring agent in the decoloring agent temporary storage tank 17b is metered by the metering addition rotary valve 17c and continuously enters the static mixing structure at the top of the decoloring reaction section 17d to be fully mixed with the raw oil. The decoloring reaction section 17d works in a vacuum state. After the extracted gas is extracted from the decoloring reaction section 17d, it is first subjected to gas-liquid separation in the gas-liquid separator 20. The gas phase part discharged from the top of the gas-liquid separator 20 enters the vacuum system through the decoloring vacuum pipe G14, and the oil droplets separated from the bottom of the gas-liquid separator 20 flow back to the decoloring reaction section 17d under the action of gravity along the separator oil return pipe.

[0131] When the decoloring filter 18 is in operation, the decoloring oil sent by the filter feeding pump P15 enters the oil inlet of the decoloring filter 18, which is connected to the side wall of the lower cone of the decoloring filter 18, gradually fills the decoloring filter 18 in operation, discharges the gas in the decoloring filter 18, and extracts the system through the decoloring vacuum extraction pipe G14 at the top of the intermediate oil tank 17e; until the overflow of the top flow return oil pipe G15 at the upper outlet of the shell of the decoloring filter 18 to the intermediate oil tank 17e, at which time the upper outlet of the shell of the decoloring filter 18 is closed.

[0132] Then the oil liquid filtered through the filter element is discharged from the intermediate oil outlet of the decoloring filter 18, and returned to the decoloring reaction section 17d through the intermediate circulating pipe G16 for circulation. After a period of operation, when the filter cake adheres to the outer periphery of the filter element of the decoloring filter 18 is stable, and the oil outlet at the intermediate oil outlet meets the requirements, the inlet valve of the intermediate circulating pipe G16 is closed, and the valve of the decoloring oil output pipe G19 is opened, and the filtered clean oil is transported into the next section through the decoloring oil output pipe G19.

[0133] When the filter cake intercepted by the filter element of the decoloring filter 18 in operation is relatively thick, the filter pressure difference is relatively large due to the relatively large flow resistance, at which time the standby decoloring filter 18 is put into operation to ensure the continuous operation of the system.

[0134] The steam valve at the upper outlet of the shell of the decoloring filter 18 is opened, the dirty oil is pressed out from the intermediate oil outlet and the oil inlet of the decoloring filter 18 through the pressure of the steam, and is collected in the intermediate oil tank 17e at the bottom of the integrated combined decoloring tower 17 through the dirty oil collecting pipe G17, the vacuum extraction port at the top of the intermediate oil tank 17e is closed, and the dirty oil in the intermediate oil tank 17e flows back to the decoloring reaction section 17d under the action of vacuum along the siphon return oil pipe G18, and is recycled and utilized.

[0135] Oil deodorization is based on the great difference in volatility between oil (triglyceride) and substances affecting the flavor, odor, color and stability of oil. The specific method for deodorization is physical distillation by spraying direct steam into oil under high vacuum and high temperature. In a high vacuum environment, the vapor pressure difference between oil and volatile impurities can be increased, and oxidation of high-temperature oil can be prevented or reduced. High temperature of oil not only increases the vapor pressure difference in the deodorization environment, but also destroys pigment substances such as carotenoids, i.e. produces a heat-sensitive decolorization effect. The production process of distillation is that water vapor passes through the high-temperature oil layer containing odor components under high vacuum, gas-liquid forms sufficient surface contact, odor components in oil volatilize into water vapor bubbles, and according to the ratio of their partial pressure, the odor components overflow into the vacuum system and are discharged, thereby realizing the deodorization of oil.

[0136] As Figure 8As shown, the deodorization section in the present application comprises an integrated combined deodorization tower 21, a falling film economizer 22, a falling film heater 23 and a water cooler B 24. The integrated combined deodorization tower 21 is sequentially provided from top to bottom with a fatty acid trap 21a, a post-deacidification tower section 21b, a pre-deacidification tower section 21c, a plate tower stripping section 21d and a gas stripping chamber 21e. The first embodiment is a small-capacity integrated deodorization section, and the diameter of the plate tower stripping section 21d is relatively small, so the falling film economizer 22 is externally arranged.

[0137] The deoiled oil output pipe G19 is connected to the deoiled oil inlet of the lower gas stripping chamber 21e of the integrated combined deodorization tower 21. The bottom oil outlet of the gas stripping chamber 21e is connected to the inlet of the gas stripping oil delivery pump P17. The outlet of the gas stripping oil delivery pump P17 is connected to the lower inlet of the cold side of the falling film economizer 22. The upper outlet of the cold side of the falling film economizer 22 is connected to the upper oil inlet of the pre-deacidification tower section 21c. The lower oil outlet of the pre-deacidification tower section 21c is connected to the upper oil inlet of the plate tower stripping section 21d. Each layer of the plate tower is respectively provided with an annular jet pipe or a stripping pump, and the steam inlets of the annular jet pipe or the stripping pump are respectively connected to the steam pipe G4.

[0138] The lower oil outlet of the plate tower stripping section 21d is connected to the inlet of the plate tower oil delivery pump P18. The outlet of the plate tower oil delivery pump P18 is connected to the oil inlet of the falling film heater 23. The oil outlet of the falling film heater 23 is connected to the upper oil inlet of the post-deacidification tower section 21b. The lower oil outlet of the post-deacidification tower section 21b is connected to the upper inlet of the hot side of the falling film economizer 22. The bottom deodorized oil outlet of the falling film economizer 22 is connected to the inlet of the deodorized oil delivery pump P19. The outlet of the deodorized oil delivery pump P19 is connected to the deodorized oil output pipe G20.

[0139] In addition, the top gas phase outlet of the post-deacidification tower section 21b of the integrated combined deodorization tower 21 is connected to the bottom of the fatty acid trap 21a. The top gas phase outlet of the fatty acid trap 21a is connected to the deodorization vacuum pipe G22, maintaining the negative pressure of the post-deacidification tower section 21b, the pre-deacidification tower section 21c and the plate tower stripping section 21d. The upper side wall of the gas stripping chamber 21e is independently connected to the deodorization vacuum pipe G22.

[0140] The fatty acid outlet of the fatty acid trap 21a is connected to the inlet of the fatty acid circulating pump P20. The outlet of the fatty acid circulating pump P20 has two pipelines. One is a circulating pipeline connected to the hot side inlet of the water cooler B 24. The hot side outlet of the water cooler B 24 is connected to the fatty acid inlet of the upper fatty acid trap 21a. The other is a fatty acid discharge pipe G21 connected to the fatty acid tank inlet of the auxiliary tank area.

[0141] The deodorized cold oil from the deodorized oil outlet pipe G19 enters the gas stripping chamber 21e, and the oxygen dissolved in the oil under vacuum is removed, and then the gas-stripped cold oil is sent out by the gas-stripped oil delivery pump P17, enters the cold side of the falling film economizer 22, and exchanges heat with the hot side deodorized hot oil, and the temperature is heated to above 220°C, and then the gas-stripped oil enters the pre-deacidification tower section 21c.

[0142] In the pre-deacidification tower section 21c, part of the free fatty acids are distilled and removed under deodorizing vacuum, and then enter the plate tower stripping section 21d under gravity for final high-temperature stripping and hot decolorization, and then the deodorized oil is sent out by the plate tower oil outlet delivery pump P18, enters the falling film heater 23 for heating, and the oil temperature rises to above 240°C, and then flows into the post-deacidification tower section 21b, and in the post-deacidification tower section 21b, most of the free fatty acids and a small amount of odor components are removed, and then the deodorized oil flows into the hot side of the falling film economizer 22, exchanges heat with the cold side gas-stripped cold oil, and then the deodorized oil enters the deodorized oil delivery pump P19, and is output through the deodorized oil outlet pipe G20.

[0143] The gas generated in the post-deacidification tower section 21b, the pre-deacidification tower section 21c and the plate tower stripping section 21d enters the fatty acid trap 21a at the top of the integrated combined deodorization tower 21, and the fatty acid trap 21a, the fatty acid circulating pump P20 and the water cooler B 24 form a fatty acid trapping system. The fatty acid circulating pump P20 sends the oil collected at the bottom of the fatty acid trap 21a to the hot side of the water cooler B 24 for cooling, and then to the top of the fatty acid trap 21a for circulating spraying, so that the fatty acid gas distilled from the deodorization section is fully trapped. When the total amount of fatty acid in the trapping system reaches the set value, part of the fatty acid is sent to the fatty acid tank outside the workshop through the fatty acid discharge pipe G21 for storage.

[0144] Figure 9 As shown in Embodiment Two, the remaining parts are the same as Embodiment One. Since the diameter of the center suction cylinder of the plate tower stripping section 21d is very large, the falling film economizer 22 is built into the center suction cylinder of the plate tower stripping section 21d, and the outer insulation layer of the falling film economizer 22 is cancelled.

[0145] As shown in Embodiment Two, the remaining parts are the same as Embodiment One. Since the diameter of the center suction cylinder of the plate tower stripping section 21d is very large, the falling film economizer 22 is built into the center suction cylinder of the plate tower stripping section 21d, and the outer insulation layer of the falling film economizer 22 is cancelled. Figure 10 As shown in Embodiment Two, the remaining parts are the same as Embodiment One. Since the diameter of the center suction cylinder of the plate tower stripping section 21d is very large, the falling film economizer 22 is built into the center suction cylinder of the plate tower stripping section 21d, and the outer insulation layer of the falling film economizer 22 is cancelled. The upper end of the plate tower stripping section cylinder is open, the lower end of the plate tower stripping section cylinder is provided with a plate tower stripping section lower head for closing it, and a partition chamber bottom plate is welded at the lower part of the inner cavity of the plate tower stripping section. The partition chamber bottom plate, the plate tower stripping section lower head and the plate tower stripping section cylinder jointly form a gas stripping chamber 21e, the top of the gas stripping chamber 21e is provided with a deodorized oil spraying pipe 21e2, the upper part of the side wall of the gas stripping chamber 21e is provided with a deodorized oil inlet 21e1, and the deodorized oil inlet 21e1 is connected with the deodorized oil spraying pipe 21e2. The upper part of the side wall of the gas stripping chamber 21e is also provided with a pre-degassing vacuum suction port 21e3, and the lower part of the plate tower stripping section lower head is provided with a gas stripping chamber oil outlet port 21e4.

[0146] The decoloring oil from the front process enters the gas separation chamber 21e from the decoloring oil inlet 21e1, is sprayed out through the decoloring oil spray pipe 21e2 and each nozzle, the air inclusions overflow, and are removed from the pre-degassing vacuum port 21e3 to avoid subsequent high-temperature oxidation of the decoloring oil.

[0147] A central air extraction cylinder is arranged upward along the axis of the plate tower stripping section cylinder from the central hole of the partition cavity bottom plate, and extends upward to the middle and upper part of the plate tower stripping section cylinder.

[0148] The falling film energy saver 22 is located in the inner cavity of the central air extraction cylinder, and the shell cavity is uniformly provided with a plurality of falling film tubes 22f. Each falling film tube 22f penetrates between the upper tube plate 22e and the lower tube plate. The upper tube port of the falling film tube 22f extends from the upper tube plate 22e and is uniformly distributed with overflow tooth grooves.

[0149] As shown in Figure 11 , the middle part of the side wall of the plate tower stripping section cylinder is connected with a falling film energy saver oil inlet pipe. The inner end of the falling film energy saver oil inlet pipe extends to the axis of the plate tower stripping section cylinder and the outlet end is bent downward to point to the center of the oil distribution plate 22b. The inner end of the falling film energy saver oil inlet pipe is provided with an oil dispersion cylinder 22a, which is beneficial to uniform overflow to the oil distribution plate 22b. The oil distribution plate 22b is fixed above the upper tube plate 22e of the falling film energy saver 22 and is parallel to each other by supporting bolts 22d. The oil distribution plate 22b is uniformly provided with a plurality of oil distribution holes. The oil distribution plate 22b is also uniformly distributed with air permeable pipes 22c penetrating through the oil layer. The gas phase removed by the falling film can enter the central air extraction cylinder above through the air permeable pipes 22c.

[0150] As shown in Figure 12 , the projection of the oil distribution hole is symmetrically distributed in a regular triangle around the upper tube port of each falling film tube 22f. The deodorizing oil is uniformly distributed to the oil distribution plate 22b through the falling film energy saver oil inlet pipe and the oil dispersion cylinder 22a. The oil distribution hole is narrow at the top and wide at the bottom to avoid blockage. The oil distribution hole uniformly distributes oil to the periphery of the falling film tube 22f, and the oil flows downward to form a falling film from the overflow tooth grooves into the inner wall of the falling film tube 22f.

[0151] The lower end of the shell of the falling film energy saver 22 penetrates the gas separation chamber 21e and the lower head of the plate tower stripping section. The lower tube plate reaches the outside of the lower head of the plate tower stripping section and is connected below with a deodorizing oil buffer tank 22j. The deodorizing oil buffer tank 22j is located in the inner cavity of the skirt. The bottom of the deodorizing oil buffer tank 22j is provided with a deodorizing oil outlet 22k.

[0152] The lower part of the shell of the falling film energy saver 22 is provided with a shell lower part inlet 22g, which is connected with the decoloring oil output pipe G19. The upper part of the shell of the falling film energy saver 22 is provided with a shell upper part outlet 22h, which is connected with the oil inlet of the pre-deacidification tower section 21c.

[0153] The pre-degassed bleached oil flows out from the gas chamber outlet 21e4 of the lower head of the plate tower stripping section, is sent into the lower shell inlet 22g of the lower part of the shell of the falling film economizer by the gas oil delivery pump P17, flows upward along the shell of the falling film economizer 22, and exchanges heat with the deodorized oil film in the tube in countercurrent, and the temperature of the deodorized oil is lowered and then is temporarily stored in the deodorized oil buffer tank 22j, and then flows out from the deodorized oil outlet 22k at the bottom of the deodorized oil buffer tank 22j. The bleached oil is preheated after heat exchange, flows out from the upper shell outlet 22h of the upper part of the shell of the falling film economizer, the upper shell outlet 22h is provided with an expansion joint, and extends radially out of the plate tower stripping section cylinder.

[0154] The annular space between the central suction cylinder and the plate tower stripping section cylinder is provided with multiple trays, and each layer of tray is provided with a stripping pump 21d4. The plate tower stripping section annular jet pipe 21d5 is arranged above the partition bottom plate, and the side wall of the plate tower stripping section cylinder of this layer is provided with a plate tower oil outlet. The plate tower stripping section annular jet pipe 21d5 and the steam inlets of the stripping pumps 21d4 are respectively connected with the steam pipe.

[0155] Generally, the trays are provided with five layers, the top of the falling film economizer 22 is flush with the top of the third layer of tray, the central suction cylinder in the center of the upper two layers of tray is disconnected with the lower part, the upper central suction cylinder is slightly smaller, and the inner diameter of the lower central suction cylinder is larger, so as to accommodate the falling film economizer 22, and an annular gas phase passage is reserved around the falling film economizer 22. The gas phase space of each layer of tray is communicated with the inner cavity of the central suction cylinder through the vent hole, and each layer of vent hole is uniformly distributed on the circumference of the central suction cylinder and located below the upper layer of tray.

[0156] Each tray is respectively provided with a partition inner cylinder 21d1 coaxial with the plate tower stripping section cylinder, the inner side of the partition inner cylinder 21d1 is an inner annular flow channel, and the outer side of the partition inner cylinder 21d1 is an outer annular flow channel; the outer wall of the central suction cylinder and the inner wall of the plate tower stripping section cylinder are provided with a radial partition plate 21d2, the outlet of the overflow pipe 21d3 of the upper layer of tray points to the head end of the inner annular flow channel close to the radial partition plate 21d2, the tail end of the partition inner cylinder 21d1 close to the other side of the radial partition plate 21d2 is provided with a notch connected with the head end of the outer annular flow channel, and the tail end of the outer annular flow channel is provided with a tray overflow pipe 21d3 overflowing to the inner annular flow channel of the next layer.

[0157] Figure 10 、 Figure 13 The outer annular flow channel of each layer overflows to the inner annular flow channel of the next layer through the tray overflow pipe 21d3, the outer annular flow channel of a layer overflows to the inner annular flow channel of the next layer, circulates around the outer annular flow channel from the notch, and then overflows to the inner annular flow channel of the next layer, and the head end and the tail end of each layer remain unchanged.

[0158] The tray overflow pipes 21d3 of the outer ring flow channel and the inner ring flow channel are both vertically downward, the first layer of tray overflows from the inner ring flow channel to the outer ring flow channel, overflows from the outer ring flow channel to the second layer of outer ring flow channel, enters the inner ring flow channel of the layer at the gap, and overflows to the third layer of inner ring flow channel, and so on.

[0159] The inner ring flow channel of each layer overflows to the outer ring flow channel of the next layer through the tray overflow pipe 21d3, the inner ring flow channel of a layer overflows to the outer ring flow channel of the next layer, and the flow circulates once from the gap to the inner ring flow channel, and then overflows to the outer ring flow channel of the next layer, and the head and tail of each layer remain unchanged.

[0160] A plurality of stripping pumps 21d4 are arranged along the inner ring flow channel and the outer ring flow channel, which greatly prolongs the flow length of the oil on each layer of tray and prolongs the residence time, ensures that the oil is first in and first out, and avoids local stagnation of the oil, which affects the quality.

[0161] Each tray is inclined with a high outer and a low inner, and the lowest part of the tray is connected with a tray emptying pipe, the tray emptying pipe of each layer extends to the outside of the plate tower stripping section cylinder and is connected with the tray backflow port of the lower layer through an emptying valve, and the tray backflow port is located below the liquid level of the outer ring flow channel. Due to the fact that the overflow height of the tray overflow pipe 21d3 cannot be adjusted, the liquid level on each tray is fixed. Under certain process conditions, it is desired to adjust the liquid level on the tray, and the emptying valve can be opened to allow the oil of the upper layer to be discharged into the next layer through the tray emptying pipe.

[0162] The lower part of the central air cylinder is provided with an air cylinder reducing section, the upper end of the air cylinder reducing section is located below the air hole of the bottom layer, the partition bottom plate plays a role similar to that of the tray, and the upper several layers of trays are stable in liquid level, so that the stripping pump 21d4 with high liquid level requirement is arranged for stripping.

[0163] The partition bottom plate located at the bottom layer is subjected to the last stage of stripping by the plate tower stripping section annular jet pipe 21d5, and the liquid level height of the layer is convenient to adjust. The air cylinder reducing section of the layer can expand the oil storage capacity above the partition bottom plate, and better buffer effect is achieved.

[0164] The lower port of the air cylinder reducing section is provided with a liquid seal disc, and the condensate of the gas phase of the central air cylinder can directly flow into the liquid seal disc under the action of gravity, and overflow downward to form a liquid seal with the gas phase space of the gas separation chamber 21e. The liquid seal disc is provided with a liquid discharge hole, and under normal working conditions, the condensate overflows from the upper port of the liquid seal disc; during shutdown, the liquid discharge hole can slowly drain the liquid seal disc.

[0165] The gas phase material stripped by each layer of tray including the partition bottom plate of the bottom layer enters the annular space between the falling film economizer shell and the central air cylinder from the air hole at the upper part of each layer, and then upward from the edge of the plate tower stripping section liquid blocking cover.

[0166] The above merely describes the preferred embodiments of the present application, shows and describes the basic principles, main features and advantages of the present application, and does not limit the patent protection scope of the present application. It should be understood by those skilled in the art that the present application is not limited by the above embodiments. In addition to the above embodiments, other embodiments can be implemented without departing from the spirit and scope of the present application. The present application can also have various changes and improvements. Any technical solution formed by equivalent replacement or equivalent transformation falls within the scope of protection required by the present application. The scope of protection required by the present application is defined by the appended claims and their equivalents. The technical features not described in the present application can be implemented by or using existing technology, and will not be described here.

Claims

1. A plant oil integrated refining system comprising a degumming section and an alkaline refining section, characterized in that, The alkali refining section comprises an integrated combined alkali refining tower, a downstream of the alkali refining section is provided with a decoloring section, the decoloring section comprises an integrated combined decoloring tower; a downstream of the decoloring section is provided with a deodorization section, the deodorization section comprises an integrated combined deodorization tower; The integrated combined alkali refining tower is sequentially stacked from top to bottom with a water washing buffer section, a secondary acidification reaction section and an alkali reaction section, an outlet of the degumming oil output pipe is connected with a cold side inlet of a steam heater C, a cold side outlet of the steam heater C is connected with a main inlet of a static acid mixer B, an outlet of the static acid mixer B is connected with a top inlet of the secondary acidification reaction section, a bottom outlet of the secondary acidification reaction section is connected with a main inlet of a static alkali mixer B through a secondary acidification oil delivery pump, an outlet of the static alkali mixer B is connected with an upper inlet of the alkali reaction section, a bottom outlet of the alkali reaction section is connected with a cold side inlet of a steam heater D through a neutralization oil delivery pump, the cold side outlet of the steam heater D is connected with an inlet of a de-soap centrifuge, a light phase de-soap oil outlet of the de-soap centrifuge is connected with an upper end inlet of the water washing buffer section, a bottom outlet of the water washing buffer section is connected with an inlet of a water washing centrifuge, a light phase water washing oil outlet of the water washing centrifuge is connected with a water washing oil output pipe.

2. The integrated vegetable oil refining system of claim 1, wherein, The degumming section is a hydration degumming section, the hydration degumming section comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a hydration reaction section, a degumming vacuum drying section, a hot water tank and a soft water tank, an outlet of a raw oil pump is connected with a cold side inlet of a steam heater A, the cold side outlet of the steam heater A is connected with a main inlet of a static water mixer, a water inlet of the static water mixer is connected with an outlet of a process hot water pipe, an outlet of the static water mixer is connected with an upper end inlet of the hydration reaction section in the integrated combined degumming tower, a lower end outlet of the hydration reaction section is connected with an inlet of a degumming centrifuge through a hydration oil delivery pump, a light phase outlet of the degumming centrifuge is connected with an upper end inlet of the degumming vacuum drying section, an exhaust port of the degumming vacuum drying section is connected with a degumming vacuum pumping pipe, a bottom outlet of the degumming vacuum drying section is connected with a degumming oil output pipe through a degumming dry oil delivery pump; an outlet of the hot water tank is connected with an inlet of the process hot water pipe through a hot water pump.

3. The integrated vegetable oil refining system of claim 1, wherein, The degumming section is an acid degumming section, which comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a primary acidification reaction section, a hydration reaction section and a degumming vacuum drying section, the outlet of the raw oil pump is connected with the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected with the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected with the acid liquid pipe, the outlet of the static acid mixer A is connected with the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected with the main inlet of the static water mixer through a primary acidification oil conveying pump, the water inlet of the static water mixer is connected with the outlet of the process hot water pipe, the outlet of the static water mixer is connected with the upper end inlet of the hydration reaction section in the integrated combined degumming tower, the lower end outlet of the hydration reaction section is connected with the inlet of the degumming centrifuge through a hydration oil conveying pump, the light phase outlet of the degumming centrifuge is connected with the upper end inlet of the degumming vacuum drying section, the exhaust port of the degumming vacuum drying section is connected with the degumming vacuum pipe, and the bottom outlet of the degumming vacuum drying section is connected with the degumming oil output pipe through a degumming dry oil conveying pump.

4. The integrated vegetable oil refining system of claim 3, wherein: The outlet of the primary acidification oil conveying pump is connected with the hot side inlet of the water cooler A, the hot side outlet of the water cooler A is connected with the main inlet of the static water mixer, and the water inlet of the static water mixer is also connected with the lye pipe; the outlet of the hydration oil conveying pump is connected with the cold side inlet of the steam heater B, and the cold side outlet of the steam heater B is connected with the inlet of the degumming centrifuge.

5. The integrated vegetable oil refining system of claim 1, wherein, The degumming section is an enzymatic degumming section, which comprises an integrated combined degumming tower, the integrated combined degumming tower is sequentially stacked from top to bottom with a primary acidification reaction section, an enzyme reaction section and a vacuum drying section, the outlet of the raw oil pump is connected with the cold side inlet of the steam heater A, the cold side outlet of the steam heater A is connected with the main inlet of the static acid mixer A, the acid inlet of the static acid mixer A is connected with the acid liquid pipe, the outlet of the static acid mixer A is connected with the top inlet of the primary acidification reaction section, the bottom outlet of the primary acidification reaction section is connected with the hot side inlet of the water cooler A through a primary acidification oil conveying pump, the hot side outlet of the water cooler A is connected with the main inlet of the static alkali mixer A, the lye inlet of the static alkali mixer A is connected with the lye pipe, the outlet of the static alkali mixer A is connected with the outlet of the enzyme preparation pipe, and the inlet of the enzyme mixer is connected with the inlet of the enzyme mixer, the outlet of the enzyme mixer is connected with the upper end inlet of the enzyme reaction section, the lower end outlet of the enzyme reaction section is connected with the cold side inlet of the steam heater B through an enzyme reaction section oil outlet pump, the cold side outlet of the steam heater B is connected with the inlet of the degumming centrifuge, the light phase outlet of the degumming centrifuge is connected with the upper end inlet of the vacuum drying section, the exhaust port of the vacuum drying section is connected with the degumming vacuum pipe, and the bottom outlet of the vacuum drying section is connected with the degumming oil output pipe through a degumming dry oil conveying pump.

6. The integrated vegetable oil refining system according to any one of claims 2 to 5, wherein: The lower part of the hot water tank is also provided with a soft water tank, the outlet of the soft water tank is connected with the inlet of a soft water pump, the outlet of the soft water pump is connected with the water supplement inlet of the hot water tank and the flushing inlet of the degumming centrifuge through a soft water pipeline.

7. The integrated vegetable oil refining system of claim 1, wherein, The integrated combined decoloring tower is sequentially stacked from top to bottom with a pulse dust collector, a decoloring agent temporary storage tank and a decoloring reaction section, the decoloring reaction section includes a static mixing structure at the upper part and a stirring decoloring section at the lower part; The inlet of the decoloring agent temporary storage tank is connected with the outlet of a decoloring agent conveying pipe, the top outlet of the decoloring agent temporary storage tank is connected with the inlet of the pulse dust collector, the top outlet of the pulse dust collector is connected with the atmosphere through a dust removal fan; The bottom outlet of the decoloring agent temporary storage tank is connected with the decoloring agent inlet of the static mixing structure through a metering addition rotary valve; the outlet of an alkaline refined oil output pipe is connected with the cold side inlet of a steam heater E, the cold side outlet of the steam heater E is connected with the oil liquid inlet of the static mixing structure; the bottom outlet of the stirring decoloring section is connected with the oil inlet of a decoloring filter through a filter feeding pump, the middle oil outlet of the decoloring filter is connected with a decoloring oil output pipe.

8. The integrated vegetable oil refining system of claim 7, wherein, The bottom part of the integrated combined decoloring tower is provided with an intermediate oil tank, at least two decoloring filters are connected in parallel, the oil inlets and the middle oil outlets of the decoloring filters are respectively connected with a dirty oil collecting pipe through valves, the outlet of the dirty oil collecting pipe is connected with the upper inlet of the intermediate oil tank, the bottom outlet of the intermediate oil tank is connected with the upper oil return inlet of the stirring decoloring section through a siphon oil return pipe.

9. The integrated vegetable oil refining system of claim 7, wherein, The stirring decoloring section is a steam stirring decoloring section or a jet stirring decoloring section.

10. The integrated vegetable oil refining system of claim 7, wherein, The upper part side wall air outlet of the stirring decoloring section is connected with the inlet of a gas-liquid separator, the top outlet of the gas-liquid separator is connected with a decoloring vacuum pipe, the bottom outlet of the gas-liquid separator is connected with the upper oil return inlet of the stirring decoloring section.

11. The integrated vegetable oil refining system of claim 8, wherein, The upper part outlets of the housings of the decoloring filters are respectively connected with a top flow oil return pipe through valves, the outlet of the top flow oil return pipe is connected with the upper inlet of the intermediate oil tank, the top exhaust port of the intermediate oil tank is connected with the decoloring vacuum pipe.

12. The integrated vegetable oil refining system of claim 7, wherein, The integrated combined deodorization tower is sequentially stacked from top to bottom with a fatty acid collector, a post-deacidification tower section, a pre-deacidification tower section and a plate tower stripping section, the decoloring oil output pipe is connected with the upper inlet of a gas chamber, the bottom outlet of the gas chamber is connected with the lower shell inlet of a falling film economizer through a gas separation oil conveying pump, the upper shell outlet of the falling film economizer is connected with the oil inlet of the pre-deacidification tower section, the bottom part of the pre-deacidification tower section is connected with the upper part of the plate tower stripping section, the bottom oil outlet of the plate tower stripping section is connected with the cold side inlet of a falling film heater through a plate tower oil output conveying pump, the cold side outlet of the falling film heater is connected with the upper oil inlet of the post-deacidification tower section, the lower oil outlet of the post-deacidification tower section is connected with the hot side inlet of the falling film economizer, the hot side outlet of the falling film economizer is connected with the inlet of a deodorization oil conveying pump; the top gas phase port of the post-deacidification tower section is connected with the bottom part of the fatty acid collector, the top exhaust port of the fatty acid collector is connected with a deodorization vacuum pipe.

13. The integrated vegetable oil refining system of claim 12, wherein, The bottom liquid outlet of the fatty acid trap is connected with the inlet of a fatty acid circulating pump, the outlet of the fatty acid circulating pump is connected with the fatty acid discharge pipe and the hot side inlet of the water cooler B respectively, and the hot side outlet of the water cooler B is connected with the top spraying port of the fatty acid trap.

14. The integrated vegetable oil refining system of claim 12, wherein, The falling film economizer is arranged in the center air cylinder of the plate tower stripping section, the annular space between the center air cylinder and the plate tower stripping section cylinder is provided with multiple trays, and each tray is provided with a stripping pump; the circumference of the center air cylinder is uniformly provided with air holes to make the gas phase space of the tray communicate with the inner cavity of the center air cylinder. The inner cavity of the shell of the falling film economizer is provided with falling film tubes, the falling film tubes pass through between the upper tube plate and the lower tube plate, the upper tube plate is provided with an oil distribution plate above, the lower end of the shell of the falling film economizer passes through the lower head of the plate tower stripping section, and the lower tube plate is connected with a deodorized oil buffer tank below, and the bottom of the deodorized oil buffer tank is provided with a deodorized oil outlet.

15. The integrated vegetable oil refining system of claim 14, wherein, Each tray is provided with a partitioned inner cylinder coaxial with the plate tower stripping section cylinder, the inner side of the partitioned inner cylinder is an inner annular flow channel, and the outer side of the partitioned inner cylinder is an outer annular flow channel; a radial partition plate is arranged between the outer wall of the center air cylinder and the inner wall of the plate tower stripping section cylinder; the outlet of the overflow pipe of the upper tray is bent to point to the head end of the inner annular flow channel close to one side of the radial partition plate, and the tail end of the partitioned inner cylinder close to the other side of the radial partition plate is provided with a notch to communicate with the head end of the outer annular flow channel.

16. The integrated vegetable oil refining system of claim 15, wherein, The tail end of the outer annular flow channel is provided with a tray overflow pipe overflowing to the head end of the next layer of inner annular flow channels, or the head end of the inner annular flow channel is provided with a tray overflow pipe overflowing to the tail end of the next layer of outer annular flow channels, or the tail end of the outer annular flow channel is provided with a tray overflow pipe overflowing to the tail end of the next layer of outer annular flow channels, and the head end of the inner annular flow channel is provided with a tray overflow pipe overflowing to the head end of the next layer of inner annular flow channels.

17. The integrated vegetable oil refining system of claim 15, wherein, Each tray is arranged in an outer high and inner low inclined manner, and the lowest part of the tray is connected with a tray emptying pipe, the tray emptying pipes of each layer extend to the outside of the plate tower stripping section cylinder and are connected with the tray backflow ports of the lower layer through emptying valves, and the tray backflow ports are located below the liquid surface of the outer annular flow channel.

18. The integrated vegetable oil refining system of claim 14, wherein, The lower part of the center air cylinder is provided with an air cylinder reduced diameter section, the upper end of the air cylinder reduced diameter section is located below the air hole of the bottom layer, the lower end of the air cylinder reduced diameter section is provided with a liquid seal plate, and the liquid seal plate is provided with a liquid discharge small hole.

19. The integrated vegetable oil refining system of claim 14, wherein, The inner end of the oil inlet pipe of the falling film economizer is provided below with an oil dispersion cylinder uniformly overflowing to the oil distribution plate, the oil distribution plate is fixed above the upper tube plate of the falling film economizer through support bolts, the oil distribution plate is uniformly provided with multiple oil distribution holes which are narrow at the top and wide at the bottom, the projections of the oil distribution holes are symmetrically distributed around the upper tube ports of each falling film tube in a regular triangle shape, and the oil distribution plate is uniformly provided with gas permeation tubes penetrating through the oil layer.

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